JP6904272B2

JP6904272B2 - Liquefied fuel gas component regulator for lorry shipment

Info

Publication number: JP6904272B2
Application number: JP2018009497A
Authority: JP
Inventors: 治貴浦部; 林　謙年; 謙年林; 戸村　啓二; 啓二戸村; 桂二鑓水; 竜太淺香
Original assignee: JFE Engineering Corp
Current assignee: JFE Engineering Corp
Priority date: 2017-05-23
Filing date: 2018-01-24
Publication date: 2021-07-14
Anticipated expiration: 2038-01-24
Also published as: JP2018197334A

Description

本発明は、例えば天然ガスを液化したＬＮＧのような液化燃料ガスの成分調整装置に関し、特に液化天然ガス（ＬＮＧ）基地からローリーによって都市ガス会社に出荷するローリー出荷向け液化燃料ガスの成分調整装置に関する。 The present invention relates to a component adjusting device for liquefied fuel gas such as LNG, which is a liquefied natural gas, and particularly a component adjusting device for liquefied fuel gas for lorry shipping, which is shipped from a liquefied natural gas (LNG) terminal to a city gas company by lorry. Regarding.

液化天然ガス（ＬＮＧ）基地においては、ＬＮＧを気化させて都市ガス向けの原料ガス、及び発電向けの燃料ガスが製造されている。また、気化前のＬＮＧの一部はローリーに搭載されたタンク（ローリータンク）へと供給され、ＬＮＧ基地を持たない都市ガス会社へと出荷されている。
発電向けの燃料ガスは、熱量範囲が規定されているわけではなく、通常は熱量調整を行わずに供給されている。
他方、都市ガスは規定の性状を満足するように、都市ガス向け燃料ガスの熱量が規定値より低い場合は増熱剤（ＬＰＧ等）を混合して熱量調整する必要があり、そのコストが都市ガス会社の負担となっている。とりわけＬＮＧをローリーで受け入れ、都市ガスとして供給しているサテライト基地では熱量調整装置の増熱能力が小さいところが多く、予め熱量を高めたＬＮＧのローリー出荷ニーズがある。 At the liquefied natural gas (LNG) terminal, LNG is vaporized to produce raw material gas for city gas and fuel gas for power generation. In addition, a part of LNG before vaporization is supplied to a tank (lorry tank) mounted on a lorry and shipped to a city gas company that does not have an LNG base.
The fuel gas for power generation does not have a specified calorific value range, and is usually supplied without calorific value adjustment.
On the other hand, in order to satisfy the specified properties of city gas, if the calorific value of the fuel gas for city gas is lower than the specified value, it is necessary to mix a heating agent (LPG, etc.) to adjust the calorific value, and the cost is urban. It is a burden on the gas company. In particular, satellite bases that accept LNG by lorry and supply it as city gas often have a small heat increasing capacity of the heat quantity adjusting device, and there is a need for LNG lorry shipment in which the amount of heat is increased in advance.

ローリータンクへ供給されるＬＮＧの熱量を高める方法として、熱量調整が要求されない発電向け液化燃料ガスからプロパン、ブタン等の重質成分を多く含む液相を分離回収し、液-液混合により増熱するものが例えば特許文献１に開示されている。
特許文献１においては、ＬＮＧを気化させた天然ガス（ＮＧ）から重質成分を分離回収する分離回収装置として蒸留装置、ガス分離装置、吸着装置が実施の形態に開示されている。
また、炭化水素混合ガスから重質成分を多く含むガスを分離し、気-気混合によって重質成分を濃縮する技術が例えば特許文献２に開示されている。 As a method of increasing the calorific value of LNG supplied to the lorry tank, a liquid phase containing a large amount of heavy components such as propane and butane is separated and recovered from the liquefied fuel gas for power generation that does not require calorific value adjustment, and the heat is increased by liquid-liquid mixing. For example, Patent Document 1 discloses what is to be done.
In Patent Document 1, a distillation device, a gas separation device, and an adsorption device are disclosed in embodiments as separation and recovery devices for separating and recovering heavy components from natural gas (NG) vaporized from LNG.
Further, for example, Patent Document 2 discloses a technique of separating a gas containing a large amount of heavy components from a hydrocarbon mixed gas and concentrating the heavy components by air-air mixing.

特許第５６５３５６３号公報Japanese Patent No. 5653563 特表２００９−５３２５６５号公報Special Table 2009-532565

特許文献１に開示された蒸留装置は設備構成が複雑でありコストが高くなるし、吸着装置はバッチ式であるため、連続処理を行うには複数の吸着装置を組み合わせる必要があり構成が複雑でコストが高くなるという問題がある。 The distillation apparatus disclosed in Patent Document 1 has a complicated equipment configuration and high cost, and since the adsorption apparatus is a batch type, it is necessary to combine a plurality of adsorption apparatus for continuous processing, and the configuration is complicated. There is a problem that the cost becomes high.

他方、ガス分離装置は装置構造が単純でコストが低いという利点がある。なお、ガス分離装置に使用される分離膜は、ガスの種類によって透過しやすさが異なる性質を利用して多成分系ガスから特定成分のガスを分離するものであり、例えばゴム状高分子膜やガラス状高分子膜などがある。膜を透過して流出してくるガス（透過ガス）には、透過しやすいガス成分が濃縮されている。一方、膜を透過しないで流出してくるガス（非透過ガス）には、逆に透過しにくいガス成分が濃縮されている。膜を透過する際には圧力損失が生じ、透過ガスの圧力は、分離膜に供給される供給ガスの圧力より低下することになる。非透過ガスも多少の圧力低下は生じるが、その程度は透過ガスの圧力低下に比較して非常に小さい。 On the other hand, the gas separation device has an advantage that the device structure is simple and the cost is low. The separation membrane used in the gas separation device separates a gas having a specific component from a multi-component gas by utilizing the property that the permeability differs depending on the type of gas. For example, a rubber-like polymer membrane. And glassy polymer membranes. The gas that easily permeates is concentrated in the gas that permeates the membrane and flows out (permeated gas). On the other hand, the gas that flows out without penetrating the membrane (non-permeable gas) is concentrated with a gas component that is difficult to permeate. When permeating through the membrane, a pressure loss occurs, and the pressure of the permeated gas becomes lower than the pressure of the supply gas supplied to the separation membrane. The non-permeated gas also causes a slight pressure drop, but the degree of the pressure drop is very small as compared with the pressure drop of the permeated gas.

ガス分離装置を用いたローリー出荷向け液化燃料ガスの熱量調整方法として、特許文献１の図５に開示されたガス分離装置を用いた熱量調整プロセスの応用が考えられるが、このプロセスは、ＬＮＧを完全に気化させた気化ガスに対して、重質成分を多く含むガスを混合して熱量調整を行っているため、熱量調整後は同様にガスの状態である。このためローリーにＬＮＧとして供給するには、熱量調整したガスを再液化させることが必須であり、液化のために大きな消費動力がかかる。 As a method for adjusting the calorific value of liquefied fuel gas for lorry shipment using a gas separator, an application of the calorific value adjusting process using the gas separator disclosed in FIG. 5 of Patent Document 1 can be considered. Since the calorific value is adjusted by mixing a gas containing a large amount of heavy components with the completely vaporized gas, the gas is in the same state after the calorific value adjustment. Therefore, in order to supply LNG to the lorry, it is essential to reliquefy the gas whose calorific value has been adjusted, and a large amount of power is consumed for liquefaction.

また、分離膜を用いたガス分離装置は、分離するために透過側の圧力を装置入口より低くする、すなわち差圧を確保する必要がある。膜透過の差圧を確保する手段として、もともと圧力の低い昇圧装置の吸込側に透過ガスを戻すことが考えられ、そのようなプロセスの例が特許文献２に開示されている（特許文献２の図２参照）。
しかし、特許文献２に開示されているような気-気混合ではローリー出荷するためにガスの液化を行う必要があり、大きな消費動力がかかる。 Further, in the gas separation device using the separation membrane, it is necessary to lower the pressure on the permeation side from the device inlet, that is, to secure the differential pressure in order to separate. As a means for ensuring the differential pressure permeating the membrane, it is conceivable to return the permeated gas to the suction side of the booster having a low pressure originally, and an example of such a process is disclosed in Patent Document 2 (Patent Document 2). (See FIG. 2).
However, in the air-air mixture as disclosed in Patent Document 2, it is necessary to liquefy the gas in order to ship the lorry, which requires a large consumption power.

本発明はかかる課題を解決するためになされたものであり、液化燃料ガスから重質成分を膜分離装置で分離し、分離された重質成分を混合することで成分調整するに際して消費動力が大きくなることなく効率的に重質成分を分離して混合調整することができるローリー出荷向け液化燃料ガスの成分調整装置を提供することを目的としている。 The present invention has been made to solve such a problem, and a large amount of power is consumed when the heavy components are separated from the liquefied fuel gas by a membrane separation device and the separated heavy components are mixed to adjust the components. It is an object of the present invention to provide a component adjusting device for liquefied fuel gas for lorry shipment, which can efficiently separate and mix and adjust heavy components without becoming.

（１）本発明に係るローリー出荷向け液化燃料ガスの成分調整装置は、液化燃料タンクから送出された液化燃料ガスが流れる液化燃料ガスラインと、該液化燃料ガスラインが分岐した、重質成分が希薄となった低発熱量ガスを供給するための第一ラインと、重質成分が濃縮された高発熱量液化燃料ガスをローリーに搭載されたローリータンクへ供給するための第二ラインとを備え、
前記第一ラインは、液化燃料ガスを昇圧する昇圧ポンプと、昇圧された液化燃料ガスを気化する気化器と、気化されたガスから重質成分を分離する膜分離装置とを有し、
前記第二ラインは、前記膜分離装置で分離された重質成分が濃縮された濃縮ガスを前記液化燃料ガスに混合する気液混合装置と、該気液混合装置で混合された混合液を前記ローリータンクの耐圧以下の圧力に減圧する減圧装置とを有し、
前記膜分離装置で分離された重質成分が濃縮された濃縮ガスを前記気液混合装置に供給する濃縮ガス供給ラインとを備えたことを特徴とするものである。 (1) The liquefied fuel gas component adjusting device for lorry shipment according to the present invention has a liquefied fuel gas line through which the liquefied fuel gas sent from the liquefied fuel tank flows and a heavy component obtained by branching the liquefied fuel gas line. It has a first line for supplying diluted low calorific value gas and a second line for supplying high calorific value liquefied fuel gas with concentrated heavy components to the lorry tank mounted on the lorry. ,
The first line has a booster pump for boosting the liquefied fuel gas, a vaporizer for vaporizing the boosted liquefied fuel gas, and a membrane separator for separating heavy components from the vaporized gas.
The second line includes a gas-liquid mixing device that mixes a concentrated gas in which a heavy component separated by the membrane separation device is concentrated with the liquefied fuel gas, and a mixed solution mixed by the gas-liquid mixing device. It has a decompression device that depressurizes the pressure below the withstand voltage of the lorry tank.
It is characterized by including a concentrated gas supply line for supplying the concentrated gas in which the heavy components separated by the membrane separation device are concentrated to the gas-liquid mixing device.

（２）また、上記（１）に記載のものにおいて、前記第一ラインにおける前記昇圧ポンプの下流側に熱交換器を設け、前記濃縮ガス供給ラインを流れる濃縮ガスを前記熱交換器によって前記第一ラインを流れる液化燃料ガスの冷熱で冷却して前記気液混合装置に供給するようにしたことを特徴とするものである。 (2) Further, in the above (1), a heat exchanger is provided on the downstream side of the booster pump in the first line, and the concentrated gas flowing through the concentrated gas supply line is subjected to the heat exchanger by the heat exchanger. It is characterized in that it is cooled by the cold heat of the liquefied fuel gas flowing through one line and supplied to the gas-liquid mixing device.

（３）また、上記（１）又は（２）に記載のものにおいて、前記濃縮ガス供給ラインに設けられて該濃縮ガス供給ラインを流れる濃縮ガスの量を調整する濃縮ガス制御弁と、
前記ローリータンク内の液化燃料ガスの熱量が予め定めた熱量を超えないように前記濃縮ガス制御弁を制御する制御装置とを備えたことを特徴とするものである。 (3) Further, in the above-mentioned (1) or (2), a concentrated gas control valve provided in the concentrated gas supply line and adjusting the amount of concentrated gas flowing through the concentrated gas supply line.
It is characterized by being provided with a control device for controlling the concentrated gas control valve so that the calorific value of the liquefied fuel gas in the lorry tank does not exceed a predetermined calorific value.

（４）また、上記（３）に記載のものにおいて、前記制御装置は、前記気液混合装置に供給される前記液化燃料ガスの圧力、温度、流量及び組成と、前記濃縮ガス供給ラインを流れる前記濃縮ガスの圧力、温度、流量及び組成に基づいて前記気液混合装置に供給される前記濃縮ガスの全量が前記気液混合装置で液化するように前記濃縮ガス制御弁を制御する機能をさらに備えていることを特徴とするものである。 (4) Further, in the device described in (3) above, the control device flows through the pressure, temperature, flow rate and composition of the liquefied fuel gas supplied to the gas-liquid mixing device and the concentrated gas supply line. Further, a function of controlling the concentrated gas control valve so that the total amount of the concentrated gas supplied to the gas-liquid mixing device based on the pressure, temperature, flow rate and composition of the concentrated gas is liquefied by the gas-liquid mixing device is further provided. It is characterized by having.

（５）また、上記（３）に記載のものにおいて、前記制御装置は、前記気液混合装置の下流側において該気液混合装置から排出される混合液の圧力、温度及び組成に基づいて該混合液の相状態を判定して、前記混合液が液相状態になるように前記濃縮ガス制御弁を制御する機能をさらに備えていることを特徴とするものである。 (5) Further, in the above-described (3), the control device is based on the pressure, temperature and composition of the mixed liquid discharged from the gas-liquid mixing device on the downstream side of the gas-liquid mixing device. It is characterized in that it further has a function of determining the phase state of the mixed liquid and controlling the concentrated gas control valve so that the mixed liquid is in the liquid phase state.

（６）本発明に係るローリー出荷向け液化燃料ガスの成分調整装置は、液化燃料タンクから送出された液化燃料ガスが流れる液化燃料ガスラインと、該液化燃料ガスラインが分岐した、重質成分が希薄となった低発熱量ガスを供給するための第一ラインと、重質成分が濃縮された高発熱量液化燃料ガスをローリーに搭載されたローリータンクへ供給するための第二ラインと、前記第一ラインを流れる液化燃料ガスの重質成分が濃縮された濃縮ガスを気液分離装置で気液分離して、分離された分離液を前記第二ラインに供給する濃縮ガス分離供給ラインとを備え、
前記第一ラインは、液化燃料を昇圧する昇圧ポンプと、昇圧された液化燃料ガスを気化する気化器と、気化されたガスから重質成分を分離する膜分離装置とを有し、
前記濃縮ガス分離供給ラインは、前記膜分離装置で分離された濃縮ガスを前記気液分離装置に供給する濃縮ガス供給ラインと、該濃縮ガス供給ラインに設けられて前記第一ラインを流れる液化燃料ガスの冷熱で前記濃縮ガスを冷却する熱交換器と、前記気液分離装置で分離された分離液を前記第二ラインに供給する分離液供給ラインとを有し、
前記第二ラインは、前記分離液が混合された混合液を前記ローリータンクの耐圧以下の圧力に減圧する減圧装置とを有することを特徴とするものである。 (6) The component adjusting device for the liquefied fuel gas for lorry shipment according to the present invention has a liquefied fuel gas line through which the liquefied fuel gas sent from the liquefied fuel tank flows and a heavy component obtained by branching the liquefied fuel gas line. The first line for supplying the diluted low calorific value gas, the second line for supplying the high calorific value liquefied fuel gas enriched with heavy components to the lorry tank mounted on the lorry, and the above. A concentrated gas separation supply line in which the concentrated gas in which the heavy components of the liquefied fuel gas flowing through the first line are concentrated is gas-liquid separated by a gas-liquid separator, and the separated separated liquid is supplied to the second line. Prepare,
The first line has a booster pump that boosts the liquefied fuel, a vaporizer that vaporizes the boosted liquefied fuel gas, and a membrane separation device that separates heavy components from the vaporized gas.
The concentrated gas separation and supply line includes a concentrated gas supply line that supplies the concentrated gas separated by the membrane separation device to the gas-liquid separation device, and a liquefied fuel that is provided in the concentrated gas supply line and flows through the first line. It has a heat exchanger that cools the concentrated gas with the cold heat of the gas, and a separation liquid supply line that supplies the separation liquid separated by the gas-liquid separation device to the second line.
The second line is characterized by having a pressure reducing device for reducing the pressure of the mixed liquid mixed with the separated liquid to a pressure equal to or lower than the pressure resistance of the lorry tank.

（７）また、上記（６）に記載のものにおいて、前記濃縮ガス分離供給ラインは、前記気液分離装置で分離された分離ガスを前記第一ラインに供給する分離ガス供給ラインを有し、
前記第一ラインは、前記昇圧ポンプの上流側に、第一ラインを流れる液化燃料ガスに前記分離ガスを混合する気液混合装置を有することを特徴とするものである。 (7) Further, in the above (6), the concentrated gas separation and supply line has a separation gas supply line that supplies the separation gas separated by the gas-liquid separation device to the first line.
The first line is characterized by having a gas-liquid mixing device that mixes the separated gas with the liquefied fuel gas flowing through the first line on the upstream side of the booster pump.

（８）また、上記（６）に記載のものにおいて、前記濃縮ガス供給ラインにおいて熱交換器を設ける代わりに、前記第一ラインを流れる液化燃料ガスの一部を前記昇圧ポンプの下流側から前記気液分離装置に供給する液化燃料ガス供給ラインを設けたことを特徴とするものである。 (8) Further, in the above-described item (6), instead of providing a heat exchanger in the concentrated gas supply line, a part of the liquefied fuel gas flowing through the first line is discharged from the downstream side of the booster pump. It is characterized by providing a liquefied fuel gas supply line for supplying to the gas-liquid separator.

（９）また、上記（７）に記載のものにおいて、前記濃縮ガス供給ラインにおいて熱交換器を設ける代わりに、前記第一ラインを流れる液化燃料ガスの一部を前記昇圧ポンプの下流側から前記気液分離装置に供給する液化燃料ガス供給ラインを設けたことを特徴とするものである。 (9) Further, in the above-described item (7), instead of providing a heat exchanger in the concentrated gas supply line, a part of the liquefied fuel gas flowing through the first line is discharged from the downstream side of the booster pump. It is characterized by providing a liquefied fuel gas supply line for supplying to the gas-liquid separator.

（１０）また、上記（７）に記載のものにおいて、前記分離ガス供給ラインに設けられて前記気液混合装置に供給される分離ガスの量を調整する分離ガス制御弁と、前記濃縮ガス供給ラインに設けられて前記気液分離装置に供給される濃縮ガスの量を調整する濃縮ガス制御弁と、前記分離液供給ラインに設けられて前記第二ラインに供給する分離液の量を調整する分離液制御弁と、
前記分離ガス供給ラインに供給される前記分離ガスの圧力、温度、流量及び組成と、前記第一ラインを流れる液化燃料ガスの圧力、温度、流量及び組成と、前記気液分離装置内の圧力、温度及び液面レベルをそれぞれ検出して、前記気液混合装置に供給される分離ガスの全量が前記気液混合装置で液化するように前記分離ガス制御弁を制御し、前記気液分離装置内の圧力及び液面レベルが所定の範囲内になり、かつ前記ローリータンク内の液化燃料ガスの熱量が予め定めた熱量を超えないように前記濃縮ガス制御弁及び前記分離液制御弁を制御する制御装置を備えたことを特徴とするものである。 (10) Further, in the above (7), the separation gas control valve provided in the separation gas supply line and adjusting the amount of the separation gas supplied to the gas-liquid mixing device, and the concentrated gas supply. A concentrated gas control valve provided on the line to adjust the amount of concentrated gas supplied to the gas-liquid separation device and an amount of separation liquid provided on the separation liquid supply line to adjust the amount of the separated liquid supplied to the second line are adjusted. Separation liquid control valve and
The pressure, temperature, flow rate and composition of the separation gas supplied to the separation gas supply line, the pressure, temperature, flow rate and composition of the liquefied fuel gas flowing through the first line, and the pressure in the gas-liquid separation device. The temperature and the liquid level are detected, respectively, and the separation gas control valve is controlled so that the total amount of the separation gas supplied to the gas-liquid mixing device is liquefied by the gas-liquid mixing device. Control to control the concentrated gas control valve and the separation liquid control valve so that the pressure and the liquid level of the above are within a predetermined range and the calorific value of the liquefied fuel gas in the lorry tank does not exceed a predetermined calorific value. It is characterized by being equipped with a device.

（１１）また、上記（９）に記載のものにおいて、前記分離ガス供給ラインに設けられて前記気液混合装置に供給される分離ガスの量を調整する分離ガス制御弁と、前記濃縮ガス供給ラインに設けられて前記気液分離装置に供給される濃縮ガスの量を調整する濃縮ガス制御弁と、前記液化燃料ガス供給ラインに設けられて前記気液分離装置に供給する液化燃料ガスの量を調整する液化燃料ガス制御弁と、前記分離液供給ラインに設けられて前記第二ラインに供給する分離液の量を調整する分離液制御弁と、
前記分離ガス供給ラインに供給される前記分離ガスの圧力、温度、流量及び組成と、前記第一ラインを流れる液化燃料ガスの圧力、温度、流量及び組成と、前記気液分離装置内の圧力、温度及び液面レベルをそれぞれ検出して、前記気液混合装置に供給される分離ガスの全量が前記気液混合装置で液化するように前記分離ガス制御弁を制御し、前記気液分離装置内の圧力及び液面レベルが所定の範囲内になり、かつ前記ローリータンク内の液化燃料ガスの熱量が予め定めた熱量を超えないように前記濃縮ガス制御弁、前記液化燃料ガス制御弁及び前記分離液制御弁を制御する制御装置を備えたことを特徴とするものである。 (11) Further, in the above (9), a separation gas control valve provided in the separation gas supply line and adjusting the amount of separation gas supplied to the gas-liquid mixing device, and the concentrated gas supply. A concentrated gas control valve provided on the line to adjust the amount of concentrated gas supplied to the gas-liquid separator, and an amount of liquefied fuel gas provided on the liquefied fuel gas supply line to supply the gas-liquid separator. A liquefied fuel gas control valve that adjusts the amount of the separation liquid, and a separation liquid control valve that is provided in the separation liquid supply line and adjusts the amount of the separation liquid supplied to the second line.
The pressure, temperature, flow rate and composition of the separation gas supplied to the separation gas supply line, the pressure, temperature, flow rate and composition of the liquefied fuel gas flowing through the first line, and the pressure in the gas-liquid separation device. The temperature and the liquid level are detected, respectively, and the separation gas control valve is controlled so that the total amount of the separation gas supplied to the gas-liquid mixing device is liquefied by the gas-liquid mixing device. The concentrated gas control valve, the liquefied fuel gas control valve, and the separation so that the pressure and the liquid level of the liquefied fuel gas in the lorry tank do not exceed a predetermined calorific value. It is characterized by being provided with a control device for controlling a liquid control valve.

本発明においては、第一ラインの液化燃料ガスを昇圧ポンプで昇圧して気化した燃料ガスを膜分離装置に供給し、分離された濃縮ガスを昇圧されていない第二ラインの液化燃料ガスに供給するようにしたことで、膜分離装置における供給側と透過側で差圧を十分とることができ、膜分離圧力差が十分に確保され、分離効率を向上することができる。しかも、第一ラインによる昇圧ポンプでの昇圧は液状態での昇圧であり、流体の昇圧動力はガス状態より液状態の方がはるかに小さいため、ガス圧縮機を用いる場合に比べてプロセスの消費動力を低く抑えられる。 In the present invention, the liquefied fuel gas of the first line is boosted by a booster pump to supply the vaporized fuel gas to the membrane separation device, and the separated concentrated gas is supplied to the liquefied fuel gas of the second line which is not pressurized. By doing so, it is possible to obtain a sufficient differential pressure between the supply side and the permeation side in the membrane separation device, a sufficient difference in the membrane separation pressure can be secured, and the separation efficiency can be improved. Moreover, the boosting by the booster pump by the first line is the boosting in the liquid state, and the boosting power of the fluid is much smaller in the liquid state than in the gas state, so the process consumption is much larger than when using a gas compressor. Power can be kept low.

本発明の実施の形態１の液化燃料ガスの成分調整装置の説明図である。It is explanatory drawing of the component adjustment apparatus of the liquefied fuel gas of Embodiment 1 of this invention. 本発明の実施の形態１の液化燃料ガスの成分調整装置の他の態様の説明図である。It is explanatory drawing of another aspect of the component adjustment apparatus of the liquefied fuel gas of Embodiment 1 of this invention. 本発明の実施の形態２の液化燃料ガスの成分調整装置の説明図である。It is explanatory drawing of the component adjustment apparatus of the liquefied fuel gas of Embodiment 2 of this invention. 本発明の実施の形態２の液化燃料ガスの成分調整装置の他の態様の説明図である（その１）。It is explanatory drawing of another aspect of the component adjustment apparatus of the liquefied fuel gas of Embodiment 2 of this invention (the 1). 本発明の実施の形態２の液化燃料ガスの成分調整装置の他の態様の説明図である（その２）。It is explanatory drawing of another aspect of the component adjustment apparatus of the liquefied fuel gas of Embodiment 2 of this invention (the 2). 本発明の実施の形態２の液化燃料ガスの成分調整装置の他の態様の説明図である（その３）。It is explanatory drawing of another aspect of the component adjustment apparatus of the liquefied fuel gas of Embodiment 2 of this invention (the 3). 本発明の実施の形態１、２の液化燃料ガスの成分調整装置の他の態様の説明図である。It is explanatory drawing of another aspect of the component adjustment apparatus of the liquefied fuel gas of Embodiments 1 and 2 of this invention. 本発明の実施の形態３の液化燃料ガスの成分調整装置の説明図である。It is explanatory drawing of the component adjustment apparatus of the liquefied fuel gas of Embodiment 3 of this invention. 本発明の実施の形態４の液化燃料ガスの成分調整装置の説明図である。It is explanatory drawing of the component adjustment apparatus of the liquefied fuel gas of Embodiment 4 of this invention.

［実施の形態１］
本発明のローリー出荷向け液化燃料ガスの成分調整装置１（以下、単に「成分調整装置１」という場合あり）を、貯留槽（ＬＮＧタンク３）に貯留されたＬＮＧを液化燃料ガスとして送出するラインを例に挙げて説明する。
したがって、本実施の形態では、ＬＮＧが本発明の液化燃料ガスに相当する。ＬＮＧはメタンを主成分とし、この他に重質成分としてエタン、プロパン、ブタン等が含まれている。よって、重質成分が希薄となったガスが低発熱量ガスであり、逆に重質成分が濃縮されたものが高発熱量ＬＮＧである。
そして、第一ラインは重質成分が希薄となった低発熱量ガスを発電所等へ供給するラインであり、第二ラインは重質成分が濃縮された高発熱量ＬＮＧをローリータンクに供給するラインである。 [Embodiment 1]
A line for delivering the LNG stored in the storage tank (LNG tank 3) as the liquefied fuel gas to the component adjusting device 1 of the liquefied fuel gas for lorry shipment of the present invention (hereinafter, may be simply referred to as “component adjusting device 1”). Will be described as an example.
Therefore, in the present embodiment, LNG corresponds to the liquefied fuel gas of the present invention. LNG contains methane as a main component, and also contains ethane, propane, butane and the like as heavy components. Therefore, the gas in which the heavy component is diluted is the low calorific value gas, and conversely, the gas in which the heavy component is concentrated is the high calorific value LNG.
The first line is a line that supplies low calorific value gas with diluted heavy components to a power plant, etc., and the second line is a line that supplies high calorific value LNG with concentrated heavy components to a lorry tank. It is a line.

本実施の形態のローリー出荷向け液化燃料ガスの成分調整装置１は、図１に示すように、液化燃料タンクとしてのＬＮＧタンク３からＬＮＧ送出ポンプ５によって例えば1.0MPaGに昇圧されて送出されたＬＮＧが流れる液化燃料ガスライン７と、液化燃料ガスライン７が分岐した、低発熱量ガスを供給するための第一ライン９と、重質成分が濃縮された高発熱量ＬＮＧをローリー１１に供給する第二ライン１３とを備えている。 As shown in FIG. 1, the component adjusting device 1 for liquefied fuel gas for lorry shipment according to the present embodiment is LNG that is boosted to, for example, 1.0 MPaG from the LNG tank 3 as the liquefied fuel tank by the LNG delivery pump 5. The liquefied fuel gas line 7 through which the gas flows, the first line 9 for supplying a low calorific value gas branched from the liquefied fuel gas line 7, and the high calorific value LNG enriched with heavy components are supplied to the lorry 11. It has a second line 13.

そして、第一ライン９にはＬＮＧを昇圧する昇圧ポンプ１５と、昇圧されたＬＮＧを気化する気化器１７と、気化されたガスから重質成分を分離する膜分離装置１９とを設けている。
また、第二ライン１３には、膜分離装置１９で分離された重質成分が濃縮された濃縮ガスをＬＮＧに混合する気液混合装置２１と、気液混合装置２１で混合された混合液をローリータンク２３の耐圧以下の圧力に減圧する減圧装置２５とを設けている。
さらに、膜分離装置１９で分離された重質成分が濃縮された濃縮ガスを気液混合装置２１に供給する濃縮ガス供給ライン２７と、ローリータンク２３で気化したガスをＬＮＧタンク３に戻すためのリターンガスライン２９とを有している。 The first line 9 is provided with a booster pump 15 for boosting LNG, a vaporizer 17 for vaporizing the boosted LNG, and a membrane separation device 19 for separating heavy components from the vaporized gas.
Further, in the second line 13, a gas-liquid mixing device 21 that mixes the concentrated gas in which the heavy components separated by the membrane separation device 19 are concentrated with LNG, and a mixed solution mixed by the gas-liquid mixing device 21 are provided. A pressure reducing device 25 for reducing the pressure to a pressure equal to or lower than the pressure resistance of the lorry tank 23 is provided.
Further, a concentrated gas supply line 27 for supplying the concentrated gas in which the heavy components separated by the membrane separation device 19 are concentrated to the gas-liquid mixing device 21 and a gas vaporized in the lorry tank 23 for returning to the LNG tank 3. It has a return gas line 29.

またさらに、本実施の形態では、濃縮ガス供給ライン２７に濃縮ガス制御弁３１を設け、ローリータンク２３内のＬＮＧの熱量が、ローリー出荷先の都市ガスの規定する熱量範囲の上限を超えないように濃縮ガス制御弁３１を制御する制御装置３３を設けている。
なお、本実施の形態の例えば昇圧ポンプ１５等の各機器類は制御装置３３又は図示しない制御装置によって運転制御される。
以下、第一ライン９及び第二ライン１３に設置される各機器を詳細に説明する。 Further, in the present embodiment, the concentrated gas control valve 31 is provided in the concentrated gas supply line 27 so that the calorific value of LNG in the lorry tank 23 does not exceed the upper limit of the calorific value range specified by the city gas to which the lorry is shipped. Is provided with a control device 33 for controlling the concentrated gas control valve 31.
Each device such as the booster pump 15 of the present embodiment is operated and controlled by the control device 33 or a control device (not shown).
Hereinafter, each device installed on the first line 9 and the second line 13 will be described in detail.

＜第一ラインに設置される機器＞
《昇圧ポンプ》
昇圧ポンプ１５は、第一ライン９を流れるＬＮＧを発電所等に向けて送出するために昇圧するポンプである。昇圧ポンプ１５によってＬＮＧは例えば7.0MPaGに昇圧される。 <Equipment installed on the first line>
《Boost pump》
The booster pump 15 is a pump that boosts the LNG flowing through the first line 9 in order to send it to a power plant or the like. LNG is boosted to, for example, 7.0 MPaG by the booster pump 15.

《気化器》
気化器１７は、昇圧ポンプ１５から送出されるＬＮＧを完全に気化させる装置である。気化器１７には、例えば海水を加熱媒体とするものが使用できるが、特にその形式は問わない。《Vaporizer》
The vaporizer 17 is a device that completely vaporizes the LNG delivered from the booster pump 15. As the vaporizer 17, for example, one using seawater as a heating medium can be used, but the type thereof is not particularly limited.

《膜分離装置》
本実施例では、ＬＮＧを構成する成分ガスのうち、エタン、プロパン、ブタン等の重質成分が透過しやすい膜を使用した場合を示す。
膜分離装置１９は、気化器１７で気化されたＮＧ（天然ガス）を、ガス分離膜を介することで、非透過側で得られるメタンリッチの低発熱量ガスと、透過側で得られるエタン、プロパン、ブタン等の重質成分が濃縮された濃縮ガスとに分離する。分離されたメタンリッチの低発熱量ガスは発電所等へ供給され、濃縮ガスは、濃縮ガス供給ライン２７に送られる。 << Membrane separation device >>
In this example, a film is used in which heavy components such as ethane, propane, and butane are easily permeated among the component gases constituting LNG.
In the membrane separation device 19, NG (natural gas) vaporized by the vaporizer 17 is passed through a gas separation membrane to obtain a methane-rich low calorific value gas obtained on the non-permeate side and ethane obtained on the permeate side. Heavy components such as propane and butane are separated into concentrated gas. The separated methane-rich low calorific value gas is supplied to a power plant or the like, and the concentrated gas is sent to the concentrated gas supply line 27.

＜第二ラインに設置される機器＞
《気液混合装置》
気液混合装置２１は、膜分離装置１９で分離された重質成分が濃縮された濃縮ガスをＬＮＧに混合するものであり、前記液体に前記気体を混合、溶解、あるいは前記気体を液化させるものであればその形態は特に限定されない。 <Equipment installed on the second line>
<< Gas-liquid mixer >>
The gas-liquid mixing device 21 mixes a concentrated gas in which the heavy components separated by the membrane separation device 19 are concentrated with LNG, and mixes, dissolves, or liquefies the gas with the liquid. If so, the form is not particularly limited.

気液混合装置２１においては、被混合液の過冷度（顕熱）が、混合ガスである濃縮ガスの凝縮潜熱を上回っている場合に、濃縮ガスが完全に液化する。本実施の形態ではＬＮＧ送出ポンプ５によって混合前の第二ライン１３のＬＮＧの過冷度を増加させているが、ＬＮＧが予め十分な過冷度を持っている場合はＬＮＧ送出ポンプ５を省略してもよい。
また、気液混合装置２１として、液化を促進するような機構の混合装置を用いてもよい。 In the gas-liquid mixing device 21, the concentrated gas is completely liquefied when the supercooling degree (sensible heat) of the liquid to be mixed exceeds the latent heat of condensation of the concentrated gas which is the mixed gas. In the present embodiment, the LNG delivery pump 5 increases the supercooling degree of the LNG of the second line 13 before mixing, but if the LNG has a sufficient supercooling degree in advance, the LNG delivery pump 5 is omitted. You may.
Further, as the gas-liquid mixing device 21, a mixing device having a mechanism for promoting liquefaction may be used.

《減圧装置》
減圧装置２５は、気液混合装置２１で混合された混合液をローリータンク２３の耐圧以下の圧力に減圧するものである。 << Decompression device >>
The depressurizing device 25 decompresses the mixed liquid mixed by the gas-liquid mixing device 21 to a pressure equal to or lower than the pressure resistance of the lorry tank 23.

＜濃縮ガス供給ラインに設置される機器＞
《濃縮ガス制御弁》
濃縮ガス制御弁３１は、濃縮ガス供給ライン２７に設けられ、制御装置３３に制御されて、気液混合装置２１に供給する濃縮ガスの量を調整するものである。 <Equipment installed on the concentrated gas supply line>
《Concentrated gas control valve》
The concentrated gas control valve 31 is provided in the concentrated gas supply line 27 and is controlled by the control device 33 to adjust the amount of the concentrated gas supplied to the gas-liquid mixing device 21.

＜制御装置＞
制御装置３３は、ローリータンク２３内のＬＮＧの熱量が、ローリー出荷先の都市ガスの規定する熱量範囲の上限を超えないように濃縮ガス制御弁３１を制御するものであり、ローリータンク２３内のＬＮＧの組成を検知する組成検出器（Ａ）の検出値を入力して、該検出値に基づいてローリータンク２３内のＬＮＧの熱量を演算する演算部３５と、演算した熱量が上記上限を超えないように濃縮ガス制御弁３１の開度等を制御する制御部３７とを有している。 <Control device>
The control device 33 controls the concentrated gas control valve 31 so that the calorific value of LNG in the lorry tank 23 does not exceed the upper limit of the calorific value range specified by the city gas to which the lorry is shipped. The calculation unit 35, which inputs the detection value of the composition detector (A) for detecting the composition of LNG and calculates the heat amount of LNG in the lorry tank 23 based on the detection value, and the calculated heat amount exceed the above upper limit. It has a control unit 37 that controls the opening degree and the like of the concentrated gas control valve 31 so as not to be present.

制御装置３３による制御の具体例としては、例えば演算部３５によって演算した熱量が予め設定した上限値以上の場合には、制御部３７が濃縮ガス制御弁３１の開度を小さくして気液混合装置２１に供給する濃縮ガス量を少なくし、演算した熱量が予め設定した下限値以下の場合には、制御部３７が濃縮ガス制御弁３１の開度を大きくして気液混合装置２１に供給する濃縮ガス量を多くする。 As a specific example of control by the control device 33, for example, when the amount of heat calculated by the calculation unit 35 is equal to or higher than a preset upper limit value, the control unit 37 reduces the opening degree of the concentrated gas control valve 31 to mix gas and liquid. When the amount of concentrated gas supplied to the device 21 is reduced and the calculated amount of heat is equal to or less than the preset lower limit value, the control unit 37 increases the opening degree of the concentrated gas control valve 31 and supplies the gas-liquid mixing device 21. Increase the amount of concentrated gas to be used.

上記のように構成された本実施の形態の動作を、図１に基づいて説明する。
ＬＮＧタンク３からはＬＮＧ送出ポンプ５によってＬＮＧが送出され、その一部が第一ライン９に流れ、残りが第二ライン１３に流れる。
第一ライン９に流れたＬＮＧには、昇圧ポンプ１５で例えば7.0MPaGに昇圧され、気化器１７に供給されて全量が気化される。気化器１７で気化されたＮＧは膜分離装置１９に供給されて、メタンリッチの低発熱量ガスと、エタン、プロパン、ブタン等の重質成分が濃縮された濃縮ガスに分離される。そして、低発熱量ガスは発電所等へ供給され、濃縮ガスは濃縮ガス供給ライン２７に送られる。 The operation of the present embodiment configured as described above will be described with reference to FIG.
LNG is sent from the LNG tank 3 by the LNG sending pump 5, a part of which flows to the first line 9, and the rest flows to the second line 13.
The LNG flowing through the first line 9 is boosted to, for example, 7.0 MPaG by the booster pump 15 and supplied to the vaporizer 17 to vaporize the entire amount. The NG vaporized by the vaporizer 17 is supplied to the membrane separation device 19 and separated into a methane-rich low calorific value gas and a concentrated gas in which heavy components such as ethane, propane and butane are concentrated. Then, the low calorific value gas is supplied to a power plant or the like, and the concentrated gas is sent to the concentrated gas supply line 27.

濃縮ガス供給ライン２７に送られた濃縮ガスは、濃縮ガス制御弁３１の開度に応じた量が第二ライン１３の気液混合装置２１に供給される。
第二ライン１３では、ＬＮＧが気液混合装置２１に供給されており、このＬＮＧに濃縮ガス供給ライン２７から送られた濃縮ガスが供給されて混合される。このとき、膜分離装置１９に供給されるＮＧは昇圧ポンプ１５でＬＮＧ送出ポンプ５の吐出圧より昇圧されており、他方、第二ライン１３の気液混合装置２１を流れるＬＮＧはＬＮＧ送出ポンプ５の吐出圧である。このため、膜分離装置１９の供給側と透過側で差圧を十分とることができ、膜分離効率を向上することができる。すなわち、昇圧ポンプ１５による昇圧分の圧力差を膜分離に利用でき、従来技術より大きな膜分離圧力差を確保できるようになっている。
そして、膜分離は圧力差が大きいほど物質の透過速度が上昇するため、膜面積あたりの重質成分回収量の増大や透過ガス量あたりの必要膜面積の縮小が可能になる。 The amount of the concentrated gas sent to the concentrated gas supply line 27 is supplied to the gas-liquid mixing device 21 of the second line 13 in an amount corresponding to the opening degree of the concentrated gas control valve 31.
In the second line 13, LNG is supplied to the gas-liquid mixing device 21, and the concentrated gas sent from the concentrated gas supply line 27 is supplied to the LNG and mixed. At this time, the NG supplied to the membrane separation device 19 is boosted by the booster pump 15 from the discharge pressure of the LNG delivery pump 5, while the LNG flowing through the gas-liquid mixing device 21 of the second line 13 is the LNG delivery pump 5. Is the discharge pressure of. Therefore, a sufficient differential pressure can be obtained between the supply side and the permeation side of the membrane separation device 19, and the membrane separation efficiency can be improved. That is, the pressure difference due to the boosted pressure by the booster pump 15 can be used for membrane separation, and a larger membrane separation pressure difference than in the prior art can be secured.
In membrane separation, the larger the pressure difference, the higher the permeation rate of the substance, so that the amount of heavy components recovered per membrane area can be increased and the required membrane area per permeated gas can be reduced.

気液混合装置２１でＬＮＧに濃縮ガスが混合され、重質成分が増加した混合液は減圧装置２５によってローリータンク２３の耐圧以下の圧力に減圧されてローリータンク２３に供給される。ローリータンク２３内では混合液の一部が蒸発して気液分離され、低発熱量成分を多く含む蒸発ガスがリターンガスライン２９によってＬＮＧタンク３に戻される。このため、ローリータンク２３内に残留するＬＮＧがさらに高熱量となる。
ローリータンク２３内に貯留された混合液の組成が組成検出器（Ａ）で常時検出されており、検出結果が制御装置３３に入力されている。制御装置３３は組成検出器（Ａ）の検出値を入力して、該検出値に基づいてローリータンク２３内のＬＮＧの熱量を演算し、演算結果に基づいて上述したように濃縮ガス制御弁３１を制御する。 The concentrated gas is mixed with LNG in the gas-liquid mixing device 21, and the mixed solution in which the heavy components are increased is depressurized by the depressurizing device 25 to a pressure equal to or lower than the pressure resistance of the lorry tank 23 and supplied to the lorry tank 23. In the lorry tank 23, a part of the mixed liquid evaporates and gas-liquid is separated, and the evaporated gas containing a large amount of low calorific value components is returned to the LNG tank 3 by the return gas line 29. Therefore, the amount of LNG remaining in the lorry tank 23 becomes even higher.
The composition of the mixed liquid stored in the lorry tank 23 is constantly detected by the composition detector (A), and the detection result is input to the control device 33. The control device 33 inputs the detection value of the composition detector (A), calculates the amount of heat of LNG in the lorry tank 23 based on the detection value, and based on the calculation result, the concentrated gas control valve 31 as described above. To control.

以上のように、本実施の形態では、第一ライン９で昇圧して気化したＮＧを膜分離装置１９に供給し、分離された濃縮ガスを昇圧されていない第二ライン１３のＬＮＧに供給するようにしたことで、膜分離装置１９における供給側と透過側で差圧を十分とることができ、膜分離圧力差が十分に確保され、分離効率を向上することができる。
しかも、第一ライン９による昇圧ポンプ１５での昇圧は液状態での昇圧であり、流体の昇圧動力はガス状態より液状態の方がはるかに小さいため、ガス圧縮機を用いる場合に比べてプロセスの消費動力を低く抑えられる。 As described above, in the present embodiment, the NG vaporized by increasing the pressure in the first line 9 is supplied to the membrane separation device 19, and the separated concentrated gas is supplied to the LNG in the second line 13 which is not pressurized. By doing so, it is possible to obtain a sufficient differential pressure between the supply side and the permeation side in the membrane separation device 19, a sufficient difference in the membrane separation pressure can be secured, and the separation efficiency can be improved.
Moreover, the boosting by the booster pump 15 by the first line 9 is the boosting in the liquid state, and the boosting power of the fluid is much smaller in the liquid state than in the gas state. The power consumption of the gas can be kept low.

なお、ローリー出荷向けのシステムでは減圧装置２５を必ず設けるため、減圧装置２５の下流側において濃縮ガスを混合するようにすれば、上述の昇圧ポンプ１５による昇圧分に加えて減圧装置２５での減圧分だけ更に差圧を確保できるようにも思えるが、このようなプロセスは成立しない。なぜなら、減圧装置２５においてＬＮＧは減圧されて沸点に達し、一部が蒸気となった気液二相状態になる。この時液相は飽和状態であり、ガスを凝縮する余地がない。そのため濃縮ガスを減圧装置２５の下流で混合したとしても凝縮できず、ＬＮＧは増熱されない。 Since the decompression device 25 is always provided in the system for lorry shipment, if the concentrated gas is mixed on the downstream side of the decompression device 25, the depressurization by the decompression device 25 is added to the boost by the booster pump 15 described above. It seems that the differential pressure can be secured by the amount, but such a process does not hold. This is because, in the decompression device 25, LNG is decompressed and reaches the boiling point, and becomes a gas-liquid two-phase state in which a part of the LNG becomes vapor. At this time, the liquid phase is saturated and there is no room for condensing the gas. Therefore, even if the concentrated gas is mixed downstream of the decompression device 25, it cannot be condensed and the LNG is not heated.

本実施の形態では、ローリータンク２３内の熱量がローリー出荷先の都市ガスの規定する熱量範囲の上限を超えず、かつできるだけ高い熱量になるように制御しているので、ローリー出荷先での熱量調整を最小限にすることができる。
もっとも、本発明はローリータンク２３内の熱量に基づいて濃縮ガス制御弁３１を制御することを必須とするものではなく、濃縮ガス制御弁３１のない場合を排除するものではない。 In the present embodiment, the amount of heat in the lorry tank 23 is controlled so as not to exceed the upper limit of the amount of heat specified by the city gas of the lorry shipping destination and to be as high as possible. Adjustments can be minimized.
However, the present invention does not require that the concentrated gas control valve 31 be controlled based on the amount of heat in the lorry tank 23, and does not exclude the case where the concentrated gas control valve 31 is not provided.

なお、上記の説明では、ローリータンク２３内のＬＮＧの熱量を演算するのに際して、ローリータンク２３内のＬＮＧの組成を組成検出器（Ａ）で検出するようにしていたが、例えば図２に示すように、減圧装置２５の上流側に圧力検出器（Ｐ）、温度検出器（Ｔ）及び組成検出器（Ａ）を、減圧装置２５の下流側に圧力検出器（Ｐ）をそれぞれ設け、これらの検出器の検出値を制御装置３３に入力して、制御装置３３はこれらの検出値に基づいてローリータンク２３内のＬＮＧの熱量を演算するようにしてもよい。 In the above description, when calculating the calorific value of LNG in the lorry tank 23, the composition of LNG in the lorry tank 23 is detected by the composition detector (A). For example, it is shown in FIG. As described above, a pressure detector (P), a temperature detector (T) and a composition detector (A) are provided on the upstream side of the decompression device 25, and a pressure detector (P) is provided on the downstream side of the decompression device 25. The detection value of the detector may be input to the control device 33, and the control device 33 may calculate the amount of heat of LNG in the lorry tank 23 based on these detection values.

［実施の形態２］
実施の形態１では、気液混合装置２１による混合後の相状態については特に問わないものであった。つまり、濃縮ガスの供給量が多い場合には混合液に気相が混じる場合もあった。
しかし、混合液に気相が混じって気液混相流となった場合には、減圧に伴う体積流量の変動が大きいために、減圧装置２５としてこれに対応可能なものが限定される。
一方、液相流の場合には体積流量変動が小さく様々な減圧装置が使用可能である。
そこで、本実施の形態では、ローリータンク２３内での熱量の制御に加えて、気液混合装置２１において全量が液化できるように濃縮ガス制御弁３１を制御するという機能を制御装置３３に付加したものである。 [Embodiment 2]
In the first embodiment, the phase state after mixing by the gas-liquid mixing device 21 is not particularly limited. That is, when the supply amount of the concentrated gas is large, the gas phase may be mixed in the mixed solution.
However, when a gas phase is mixed with the mixed liquid to form a gas-liquid mixed phase flow, the volume flow rate fluctuates greatly with decompression, so that the decompression device 25 that can handle this is limited.
On the other hand, in the case of liquid phase flow, the volume flow rate fluctuation is small and various decompression devices can be used.
Therefore, in the present embodiment, in addition to controlling the amount of heat in the lorry tank 23, the control device 33 is provided with a function of controlling the concentrated gas control valve 31 so that the entire amount can be liquefied in the gas-liquid mixing device 21. It is a thing.

本実施の形態の成分調整装置３９を図３に基づいて説明する。なお、図３において図１と同一部分及び対応する部分には同一の符号を付して説明を省略する。
本実施の形態では、第二ライン１３における気液混合装置２１の上流側及び濃縮ガス供給ライン２７に、圧力検出器（Ｐ）、温度検出器（Ｔ）、流量検出器（Ｆ）及び組成検出器（Ａ）をそれぞれ設けている。
そして、制御装置３３における演算部３５は、これらの圧力検出器（Ｐ）、温度検出器（Ｔ）、流量検出器（Ｆ）及び組成検出器（Ａ）の検出値を入力してＬＮＧの過冷度及び濃縮ガスの凝縮潜熱を求め、全量が液化する濃縮ガスの最大混合可能量を演算する。
そして、制御部３７は、演算部３５の演算結果に基づいて気液混合装置２１に供給される濃縮ガス量が最大混合可能量以下になるように濃縮ガス制御弁３１を制御する。
このとき、濃縮ガスの混合量は、混合液の熱量が都市ガスの規定する熱量範囲の上限を超えないように制御する。 The component adjusting device 39 of the present embodiment will be described with reference to FIG. In FIG. 3, the same parts as those in FIG. 1 and the corresponding parts are designated by the same reference numerals, and the description thereof will be omitted.
In the present embodiment, the pressure detector (P), the temperature detector (T), the flow rate detector (F), and the composition detection are performed on the upstream side of the gas-liquid mixing device 21 and the concentrated gas supply line 27 in the second line 13. Each vessel (A) is provided.
Then, the calculation unit 35 in the control device 33 inputs the detection values of the pressure detector (P), the temperature detector (T), the flow rate detector (F), and the composition detector (A), and inputs the detection values of the LNG error. The coldness and latent heat of condensation of the concentrated gas are obtained, and the maximum mixable amount of the concentrated gas whose total amount is liquefied is calculated.
Then, the control unit 37 controls the concentrated gas control valve 31 so that the amount of concentrated gas supplied to the gas-liquid mixing device 21 is equal to or less than the maximum mixable amount based on the calculation result of the calculation unit 35.
At this time, the mixing amount of the concentrated gas is controlled so that the calorific value of the mixed liquid does not exceed the upper limit of the calorific value range specified by the city gas.

なお、濃縮ガス供給ライン２７の途中にバッファタンクを設けることで、濃縮ガスの分離量と混合量に差をつけられる緩衝作用を持たせるようにしてもよい。 By providing a buffer tank in the middle of the concentrated gas supply line 27, a buffering action may be provided so that the separated amount and the mixed amount of the concentrated gas can be differentiated.

本実施の形態では、気液混合装置２１による混合後の流体に気相が混じらない液相のみの流体になるので、上述したように減圧装置２５として様々な仕様のものが使用可能である。 In the present embodiment, since the fluid is only the liquid phase in which the gas phase is not mixed with the fluid after mixing by the gas-liquid mixing device 21, various specifications can be used as the depressurizing device 25 as described above.

なお、図３においては、気液混合装置２１の上流側に圧力検出器（Ｐ）を設置しているが、気液混合装置２１における圧力損失を考慮する場合には、気液混合装置２１の下流側にも圧力検出器（Ｐ）を設置して検出値を制御装置３３に入力するようにすればよい。
もっとも、気液混合装置２１の圧力損失が推定できる場合には、圧力検出器（Ｐ）を設けることなく、推定値を制御装置３３に入力してもよい。 In FIG. 3, the pressure detector (P) is installed on the upstream side of the gas-liquid mixing device 21, but when considering the pressure loss in the gas-liquid mixing device 21, the gas-liquid mixing device 21 A pressure detector (P) may be installed on the downstream side as well, and the detected value may be input to the control device 33.
However, if the pressure loss of the gas-liquid mixing device 21 can be estimated, the estimated value may be input to the control device 33 without providing the pressure detector (P).

上記の制御装置３３における制御方式は、濃縮ガス制御弁３１の制御に関していわゆるフィードフォワード制御であったが、制御装置３３による濃縮ガス制御弁３１の制御はいわゆるフィードバック制御によって行ってもよい。
具体的には、図４に示すように、気液混合装置２１の下流側に圧力検出器（Ｐ）、温度検出器（Ｔ）及び組成検出器（Ａ）を設け、これら圧力検出器（Ｐ）、温度検出器（Ｔ）及び組成検出器（Ａ）の検出値を演算部３５に入力して混合後のＬＮＧの相状態を判定し、演算部３５の演算結果に基づいて制御部３７が濃縮ガス制御弁３１を制御するようにすればよい。
制御部３７は、演算部３５の判定結果によって気液混相、あるいは気相状態になるおそれがある場合には、濃縮ガス制御弁３１を絞って気液混合装置２１に供給される濃縮ガス量を少なくする。 The control method in the control device 33 is so-called feedforward control with respect to the control of the concentrated gas control valve 31, but the control of the concentrated gas control valve 31 by the control device 33 may be performed by so-called feedback control.
Specifically, as shown in FIG. 4, a pressure detector (P), a temperature detector (T), and a composition detector (A) are provided on the downstream side of the gas-liquid mixing device 21, and these pressure detectors (P) are provided. ), The detection values of the temperature detector (T) and the composition detector (A) are input to the calculation unit 35 to determine the phase state of LNG after mixing, and the control unit 37 determines the phase state of LNG after mixing, and the control unit 37 is based on the calculation result of the calculation unit 35. The concentrated gas control valve 31 may be controlled.
When there is a possibility that a gas-liquid mixed phase or a gas phase state may occur depending on the determination result of the calculation unit 35, the control unit 37 throttles the concentrated gas control valve 31 to reduce the amount of concentrated gas supplied to the gas-liquid mixing device 21. Reduce.

また、濃縮ガス制御弁３１の制御に関しては、フィードフォワード、フィードバックの他に両者を組み合わせて制御を行うようにしてよい。 Further, regarding the control of the concentrated gas control valve 31, in addition to feedforward and feedback, both may be combined for control.

また、上記の例では、ローリータンク２３内のＬＮＧの熱量の調整に関しては、実施の形態１の図１に示したものと同様に、ローリータンク２３内のＬＮＧの組成を組成検出器（Ａ）で検出して行うものであったが、組成検出器（Ａ）に代えて全量液化の制御のために設置している検出器を利用してローリータンク２３内のＬＮＧの熱量を調整するようにしてもよい。 Further, in the above example, regarding the adjustment of the amount of heat of LNG in the lorry tank 23, the composition of LNG in the lorry tank 23 is determined by the composition detector (A) in the same manner as that shown in FIG. 1 of the first embodiment. However, instead of the composition detector (A), a detector installed for controlling total liquefaction was used to adjust the amount of heat of LNG in the lorry tank 23. You may.

例えば、全量液化に関してフィードフォワード制御を行う場合には、図５に示すように、減圧装置２５の上流側と下流側に圧力検出器（Ｐ）をそれぞれ追加して、減圧装置２５の上流側に設置した圧力検出器（Ｐ）、気液混合装置２１の上流側に設置した温度検出器（Ｔ）、組成検出器（Ａ）及び減圧装置２５の下流側に設置した圧力検出器（Ｐ）の検出値を制御装置３３に入力して、演算部３５においてこれらの検出値に基づいてローリータンク２３内のＬＮＧの熱量を演算するようにすればよい。 For example, when performing feed-forward control for total volume liquefaction, as shown in FIG. 5, pressure detectors (P) are added to the upstream side and the downstream side of the decompression device 25, respectively, and the pressure detectors (P) are added to the upstream side of the decompression device 25. Of the installed pressure detector (P), the temperature detector (T) installed on the upstream side of the gas-liquid mixing device 21, the composition detector (A), and the pressure detector (P) installed on the downstream side of the decompression device 25. The detected values may be input to the control device 33, and the calculation unit 35 may calculate the amount of heat of LNG in the lorry tank 23 based on these detected values.

また、全量液化に関してフィードバック制御を行う場合には、図６に示すように、新たな検出器を追加することなく、全量液化のために設置している減圧装置２５の上流側の圧力検出器（Ｐ）、温度検出器（Ｔ）及び組成検出器（Ａ）と、減圧装置２５の下流側の圧力検出器（Ｐ）の検出値に基づいてローリータンク２３内のＬＮＧの熱量を演算するようにしてもよい。 Further, when feedback control is performed for total volume liquefaction, as shown in FIG. 6, a pressure detector on the upstream side of the decompression device 25 installed for total volume liquefaction (without adding a new detector). The amount of heat of LNG in the lorry tank 23 is calculated based on the detection values of P), the temperature detector (T), the composition detector (A), and the pressure detector (P) on the downstream side of the decompression device 25. You may.

また、図７に示すように、第一ライン９における昇圧ポンプ１５の下流側に熱交換器４１を設置して、濃縮ガス供給ライン２７を流れる濃縮ガスと、昇圧ポンプ１５による昇圧後の第一ライン９を流れるＬＮＧとの間で熱交換することで濃縮ガスを冷却し、濃縮ガスの凝縮に必要な熱量を低減することで気液混合装置２１での濃縮ガスの最大混合可能量が増加するようにしてもよい。なお、図７においては、各検出器及び制御装置３３の図示を省略しているが、熱交換器４１による熱交換を行うことについては、上述したいずれの実施の形態においても適用可能である。 Further, as shown in FIG. 7, a heat exchanger 41 is installed on the downstream side of the booster pump 15 in the first line 9, and the concentrated gas flowing through the concentrated gas supply line 27 and the first after boosting by the booster pump 15 are installed. By exchanging heat with the LNG flowing through the line 9, the concentrated gas is cooled, and the amount of heat required for condensing the concentrated gas is reduced, so that the maximum amount of the concentrated gas that can be mixed in the gas-liquid mixing device 21 is increased. You may do so. Although the detector and the control device 33 are not shown in FIG. 7, the heat exchange by the heat exchanger 41 can be applied to any of the above-described embodiments.

また他の態様として、濃縮ガスの一部のガス、又は膜分離装置１９の下流に設けた膜分離装置１９の濃縮ガスを昇圧ポンプ１５の上流側に戻して混合するリサイクルラインを設け、第一ライン９のＬＮＧの重質成分を濃縮するようにしてもよい。膜分離は分離する物質の入口分圧が高いほど透過速度が上昇するため、膜面積あたりの重質成分回収量の増加、重質成分回収率の向上、透過ガス量あたりの必要膜面積の縮小が可能になる。 As another embodiment, a recycling line is provided in which a part of the concentrated gas or the concentrated gas of the membrane separation device 19 provided downstream of the membrane separation device 19 is returned to the upstream side of the booster pump 15 and mixed. The heavy components of LNG in line 9 may be concentrated. In membrane separation, the higher the partial pressure at the inlet of the substance to be separated, the higher the permeation rate. Therefore, the recovery amount of heavy components per membrane area is increased, the recovery rate of heavy components is improved, and the required membrane area per permeated gas amount is reduced. Becomes possible.

［実施の形態３］
実施の形態３に係る成分調整装置４３を図８に基づいて説明する。なお、図８において、実施の形態１、２を示した図１、図７と同一部分には同一の符号を付して説明を省略する。
実施の形態３に係る成分調整装置４３が実施の形態１、２と異なる主な点は、第二ライン１３に気液混合装置２１を設けることに代えて、膜分離装置１９で分離されて特定成分が濃縮された濃縮ガスを気液分離装置４９で気液分離して、分離された分離液を第二ライン１３に供給し、分離された分離ガスを第一ライン９に供給する濃縮ガス分離供給ライン４５を設けた点、及び第一ライン９に濃縮ガス分離供給ライン４５から供給される分離ガスをＬＮＧに混合するための第一気液混合装置４７を設けた点である。 [Embodiment 3]
The component adjusting device 43 according to the third embodiment will be described with reference to FIG. In FIG. 8, the same parts as those in FIGS. 1 and 7 showing the first and second embodiments are designated by the same reference numerals, and the description thereof will be omitted.
The main difference between the component adjusting device 43 according to the third embodiment and the first and second embodiments is that instead of providing the gas-liquid mixing device 21 on the second line 13, the component adjusting device 43 is separated and specified by the membrane separation device 19. Concentrated gas separation in which the concentrated gas in which the components are concentrated is gas-liquid separated by the gas-liquid separation device 49, the separated separation liquid is supplied to the second line 13, and the separated separation gas is supplied to the first line 9. A point where the supply line 45 is provided, and a point where the first gas-liquid mixing device 47 for mixing the separated gas supplied from the concentrated gas separation supply line 45 with the LNG is provided in the first line 9.

そして、濃縮ガス分離供給ライン４５は、膜分離装置１９で分離された濃縮ガスを気液分離装置４９に供給する濃縮ガス供給ライン２７と、濃縮ガス供給ライン２７に設けられて第一ライン９を流れるＬＮＧの冷熱で濃縮ガスを冷却する熱交換器４１と、気液分離装置４９で分離された分離液を第二ラインに供給する分離液供給ライン５１と、気液分離装置４９で分離された分離ガスを第一ライン９の第一気液混合装置４７に供給する分離ガス供給ライン５３とを有している。 The concentrated gas separation and supply line 45 includes a concentrated gas supply line 27 that supplies the concentrated gas separated by the membrane separation device 19 to the gas-liquid separation device 49, and a first line 9 provided in the concentrated gas supply line 27. It was separated by a heat exchanger 41 that cools the concentrated gas with the cold heat of the flowing LNG, a separation liquid supply line 51 that supplies the separation liquid separated by the gas-liquid separation device 49 to the second line, and a gas-liquid separation device 49. It has a separation gas supply line 53 that supplies the separation gas to the first gas-liquid mixing device 47 of the first line 9.

また、分離液供給ライン５１には分離液制御弁５５が、分離ガス供給ライン５３には分離ガス制御弁５７がそれぞれ設けられている。
さらに、気液分離装置４９には、圧力検出器（Ｐ）、温度検出器（Ｔ）及び液面レベル検出器（Ｌ）が設けられ、分離ガス供給ライン５３及び第一ライン９には、圧力検出器（Ｐ）、温度検出器（Ｔ）、流量検出器（Ｆ）及び組成検出器（Ａ）がそれぞれ設けられている。
またさらに、本実施の形態では、分離液制御弁５５、分離ガス制御弁５７及び濃縮ガス制御弁３１を制御して、第二ライン１３に供給する分離液量、第一気液混合装置４７に供給する分離ガス量及び気液分離装置４９に供給する濃縮ガス量を制御する第２の制御装置５９が設けられている。 Further, the separation liquid supply line 51 is provided with a separation liquid control valve 55, and the separation gas supply line 53 is provided with a separation gas control valve 57.
Further, the gas-liquid separation device 49 is provided with a pressure detector (P), a temperature detector (T), and a liquid level detector (L), and the separation gas supply line 53 and the first line 9 are provided with pressure. A detector (P), a temperature detector (T), a flow rate detector (F), and a composition detector (A) are provided, respectively.
Furthermore, in the present embodiment, the separation liquid control valve 55, the separation gas control valve 57, and the concentrated gas control valve 31 are controlled to supply the separation liquid amount to the second line 13 and the first gas-liquid mixing device 47. A second control device 59 is provided to control the amount of separated gas to be supplied and the amount of concentrated gas to be supplied to the gas-liquid separation device 49.

第２の制御装置５９は、第２演算部６１と第２制御部６３を備えている。
昇圧ポンプ１５は液ポンプであり、混合液に気相が残留しないことが望ましく、そのため第２演算部６１は、第一ライン９及び分離ガス供給ライン５３における第一気液混合装置４７の上流側に設けられた、圧力検出器（Ｐ）、温度検出器（Ｔ）、流量検出器（Ｆ）及び組成検出器（Ａ）の検出値を入力して、第一気液混合装置４７で全量が液化する混合可能な分離ガスの最大混合可能量を演算する。
また、気液分離装置４９では液面レベルをある一定範囲内に制御することが好ましく、またＬＮＧの熱量が、ローリー出荷先の都市ガスの規定する熱量範囲の上限を超えないようにする必要がある。
このため、第２演算部は、気液分離装置４９に設けられた、圧力検出器（Ｐ）、温度検出器（Ｔ）及び液面レベル検出器（Ｌ）の検出値、第一ライン９に設けられた、圧力検出器（Ｐ）、温度検出器（Ｔ）、流量検出器（Ｆ）及び組成検出器（Ａ）の検出値及びローリータンク２３内のＬＮＧの組成を検出する組成検出器（Ａ）の検出値を入力して、分離液供給ライン５１を通じての分離液の第二ライン１３への供給量を演算する。
そして、第２制御部６３は、第２演算部６１の演算結果に基づいて分離ガス制御弁５７、濃縮ガス制御弁３１及び分離液制御弁５５を制御する。 The second control device 59 includes a second calculation unit 61 and a second control unit 63.
The booster pump 15 is a liquid pump, and it is desirable that no gas phase remains in the mixed liquid. Therefore, the second calculation unit 61 is on the upstream side of the first gas-liquid mixing device 47 in the first line 9 and the separated gas supply line 53. Input the detection values of the pressure detector (P), the temperature detector (T), the flow rate detector (F), and the composition detector (A) provided in the first gas-liquid mixing device 47, and the total amount is adjusted by the first gas-liquid mixing device 47. Calculate the maximum mixable amount of liquefiable mixable separated gas.
Further, in the gas-liquid separator 49, it is preferable to control the liquid level within a certain range, and it is necessary to prevent the calorific value of LNG from exceeding the upper limit of the calorific value range specified by the city gas to which the lorry is shipped. is there.
Therefore, the second calculation unit is on the first line 9 of the detection values of the pressure detector (P), the temperature detector (T), and the liquid level detector (L) provided in the gas-liquid separation device 49. A composition detector (P), a temperature detector (T), a flow rate detector (F), and a composition detector (A) provided, and a composition detector for detecting the composition of LNG in the lorry tank 23 (A). The detection value of A) is input to calculate the supply amount of the separation liquid to the second line 13 through the separation liquid supply line 51.
Then, the second control unit 63 controls the separation gas control valve 57, the concentrated gas control valve 31, and the separation liquid control valve 55 based on the calculation result of the second calculation unit 61.

上記のように構成された本実施の形態の動作に関し、図８に基づいて、特に気液分離装置４９を設けたことに関連する点を中心に説明する。
ＬＮＧタンク３からはＬＮＧ送出ポンプ５によってＬＮＧが送出され、その一部が第一ライン９に流れ、残りが第二ライン１３に流れる。
第一ライン９に流れたＬＮＧには、昇圧ポンプ１５で例えば7.0MPaGに昇圧され、気化器１７に供給されて全量が気化される。気化器１７で気化されたＮＧは膜分離装置１９に供給されて、メタンリッチの低発熱量ガスと、エタン、プロパン、ブタン等の重質成分が濃縮された濃縮ガスに分離される。そして、低発熱量ガスは発電所等へ供給され、濃縮ガスは濃縮ガス供給ライン２７に送られる Regarding the operation of the present embodiment configured as described above, the points related to the provision of the gas-liquid separation device 49 will be described with reference to FIG.
LNG is sent from the LNG tank 3 by the LNG sending pump 5, a part of which flows to the first line 9, and the rest flows to the second line 13.
The LNG flowing through the first line 9 is boosted to, for example, 7.0 MPaG by the booster pump 15 and supplied to the vaporizer 17 to vaporize the entire amount. The NG vaporized by the vaporizer 17 is supplied to the membrane separation device 19 and separated into a methane-rich low calorific value gas and a concentrated gas in which heavy components such as ethane, propane and butane are concentrated. Then, the low calorific value gas is supplied to the power plant or the like, and the concentrated gas is sent to the concentrated gas supply line 27.

濃縮ガス供給ライン２７に送られた濃縮ガスは、濃縮ガス制御弁３１の開度に応じた量が熱交換器４１に供給される。熱交換器４１では、低温のＬＮＧと高温の濃縮ガスの間で熱交換がなされ、濃縮ガスが冷却されることで気液混合状態となり、気液分離装置４９に送られる。
気液分離装置４９では、ガスと液が分離される。ここで、元の濃縮ガス供給ライン２７よりも分離液の熱量は更に高くなる。一方、分離ガスの熱量は濃縮ガス供給ライン２７よりも低くなる。
気液分離装置４９で分離された分離ガスは分離ガス制御弁５７を通して第一気液混合装置４７に送られ、更に熱量が高まった分離液は分離液制御弁５５を通して第二ライン１３に供給される。
本実施の形態では、第二ライン１３に供給されるのは液体であるため、凝縮潜熱を必要とせず第二ライン１３に流れる液体の温度が上がりにくいという利点がある。 The concentrated gas sent to the concentrated gas supply line 27 is supplied to the heat exchanger 41 in an amount corresponding to the opening degree of the concentrated gas control valve 31. In the heat exchanger 41, heat is exchanged between the low-temperature LNG and the high-temperature concentrated gas, and the concentrated gas is cooled to enter a gas-liquid mixed state and sent to the gas-liquid separation device 49.
In the gas-liquid separation device 49, the gas and the liquid are separated. Here, the calorific value of the separation liquid is further higher than that of the original concentrated gas supply line 27. On the other hand, the calorific value of the separated gas is lower than that of the concentrated gas supply line 27.
The separated gas separated by the gas-liquid separation device 49 is sent to the first gas-liquid mixing device 47 through the separation gas control valve 57, and the separated liquid having a higher calorific value is supplied to the second line 13 through the separation liquid control valve 55. To.
In the present embodiment, since the liquid is supplied to the second line 13, there is an advantage that the temperature of the liquid flowing through the second line 13 does not easily rise without requiring latent heat of condensation.

本実施の形態では実施の形態１、２の効果に加えて以下の効果を奏することができる。
第一気液混合装置４７に供給される分離ガスの全量が液化して混合液には気相が残留しないようにしているので、昇圧ポンプ１５で効率的に送液することができる。
また、気液分離装置４９により、濃縮ガス供給ライン２７の濃縮ガスよりも更に高い熱量をもつ分離液を第二ライン１３に供給することが出来る。 In the present embodiment, the following effects can be obtained in addition to the effects of the first and second embodiments.
Since the entire amount of the separated gas supplied to the first gas-liquid mixing device 47 is liquefied so that the gas phase does not remain in the mixed liquid, the booster pump 15 can efficiently supply the liquid.
Further, the gas-liquid separation device 49 can supply the separation liquid having a higher calorific value than the concentrated gas of the concentrated gas supply line 27 to the second line 13.

［実施の形態４］
実施の形態４に係る成分調整装置６５を図９に基づいて説明する。なお、図９において、実施の形態３を示した図８と同一部分には同一の符号を付して説明を省略する。
実施の形態４に係る成分調整装置６５は、実施の形態３における熱交換器４１に代えて、第一ライン９における昇圧ポンプ１５の下流側から気液分離装置４９にＬＮＧを供給するＬＮＧ供給ライン６７を設けたものである。ＬＮＧ供給ライン６７には、ＬＮＧ供給量を調整するためのＬＮＧ制御弁６９が設けられている。 [Embodiment 4]
The component adjusting device 65 according to the fourth embodiment will be described with reference to FIG. In FIG. 9, the same parts as those in FIG. 8 showing the third embodiment are designated by the same reference numerals, and the description thereof will be omitted.
The component adjusting device 65 according to the fourth embodiment is an LNG supply line that supplies LNG to the gas-liquid separation device 49 from the downstream side of the booster pump 15 in the first line 9 instead of the heat exchanger 41 in the third embodiment. 67 is provided. The LNG supply line 67 is provided with an LNG control valve 69 for adjusting the LNG supply amount.

また、本実施の形態においても、実施の形態３と同様に、第一気液混合装置４７において供給される分離ガスの全量が液化され、気液分離装置４９では液面レベルをある一定範囲内に制御され、またＬＮＧの熱量が、ローリー出荷先の都市ガスの規定する熱量範囲の上限を超えないようにする必要がある。
そのため、本実施の形態では、第３演算部７３、第３制御部７５を有する第３の制御装置７１を備え、第３の制御装置７１は、気液分離装置４９に設けられた、圧力検出器（Ｐ）、温度検出器（Ｔ）及び液面レベル検出器（Ｌ）、第一ライン９及び分離ガス供給ライン５３における第一気液混合装置４７の上流側に設けられた、圧力検出器（Ｐ）、温度検出器（Ｔ）、流量検出器（Ｆ）及び組成検出器（Ａ）の検出値及びローリータンク２３内のＬＮＧの組成を検出する組成検出器（Ａ）の検出値を入力して、分離ガス制御弁５７、濃縮ガス制御弁３１、ＬＮＧ制御弁６９及び分離液制御弁５５を制御する。 Further, also in the present embodiment, as in the third embodiment, the entire amount of the separated gas supplied in the first gas-liquid mixing device 47 is liquefied, and the liquid level in the gas-liquid separating device 49 is within a certain range. It is necessary that the calorific value of LNG does not exceed the upper limit of the calorific value range specified by the city gas to which the lorry is shipped.
Therefore, in the present embodiment, the third control device 71 having the third calculation unit 73 and the third control unit 75 is provided, and the third control device 71 is provided in the gas-liquid separation device 49 for pressure detection. A pressure detector provided on the upstream side of the first gas-liquid mixing device 47 in the device (P), the temperature detector (T), the liquid level detector (L), the first line 9, and the separated gas supply line 53. Input the detection values of (P), temperature detector (T), flow rate detector (F) and composition detector (A), and the detection value of the composition detector (A) that detects the composition of LNG in the lorry tank 23. Then, the separation gas control valve 57, the concentrated gas control valve 31, the LNG control valve 69, and the separation liquid control valve 55 are controlled.

上記のように構成された本実施の形態の動作を図９に基づいて説明する。
本実施の形態の動作は実施の形態３とほぼ同様であるが、実施の形態３では膜分離装置１９で分離された濃縮ガスを、熱交換器４１を介して第一ライン９のＬＮＧで冷却していたのに対して、本実施の形態では第一ライン９のＬＮＧの一部を気液分離装置４９に供給することで冷却する点が異なるので、これに関連する点について以下説明する。 The operation of the present embodiment configured as described above will be described with reference to FIG.
The operation of the present embodiment is almost the same as that of the third embodiment, but in the third embodiment, the concentrated gas separated by the membrane separation device 19 is cooled by the LNG of the first line 9 via the heat exchanger 41. On the other hand, in the present embodiment, a part of the LNG of the first line 9 is supplied to the gas-liquid separation device 49 for cooling, and the points related to this will be described below.

濃縮ガス供給ライン２７に送られた濃縮ガスは、濃縮ガス制御弁３１の開度に応じた量が気液分離装置４９に送られる。また、昇圧ポンプ１５から送られたＬＮＧのうち一部は、ＬＮＧ制御弁６９の開度に応じた量が気液分離装置４９に送られる。
気液分離装置４９では、ガスと液が分離される。ここで、元の濃縮ガス供給ライン２７の濃縮ガスよりも分離液の熱量は更に高くなる。一方、分離ガスの熱量は濃縮ガス供給ライン２７の濃縮ガスよりも低くなる。
分離ガスは分離ガス制御弁５７を通して第一気液混合装置４７に送られ、更に熱量が高まった分離液は分離液制御弁５５を通して第二ライン１３に供給される。 The amount of the concentrated gas sent to the concentrated gas supply line 27 is sent to the gas-liquid separator 49 in an amount corresponding to the opening degree of the concentrated gas control valve 31. Further, a part of the LNG sent from the booster pump 15 is sent to the gas-liquid separation device 49 in an amount corresponding to the opening degree of the LNG control valve 69.
In the gas-liquid separation device 49, the gas and the liquid are separated. Here, the calorific value of the separation liquid is further higher than that of the concentrated gas of the original concentrated gas supply line 27. On the other hand, the calorific value of the separated gas is lower than that of the concentrated gas of the concentrated gas supply line 27.
The separation gas is sent to the first gas-liquid mixing device 47 through the separation gas control valve 57, and the separation liquid having a higher calorific value is supplied to the second line 13 through the separation liquid control valve 55.

本実施の形態の作用効果については、実施の形態３と同様である。 The action and effect of the present embodiment are the same as those of the third embodiment.

なお、上記の実施の形態１〜４においては、ローリータンク２３で気化したガスをＬＮＧタンク３に戻すためのリターンガスライン２９とを有している例を示したが、リターンガスライン２９は必須ではなく、ローリータンク２３で気化したガスはＬＮＧタンク３に戻すことなく、ガス燃焼ボイラなどガスの熱量の制約が緩やかな機器に供給するようにしてもよい。 In the above-described first to fourth embodiments, an example having a return gas line 29 for returning the gas vaporized in the lorry tank 23 to the LNG tank 3 is shown, but the return gas line 29 is indispensable. Instead, the gas vaporized in the lorry tank 23 may not be returned to the LNG tank 3, but may be supplied to a device such as a gas combustion boiler in which the amount of heat of the gas is loosely restricted.

また、実施の形態３、４おいては、気液分離装置４９によって気液分離された分離ガスを液化燃料ガスライン７の第一気液混合装置４７に供給する例を示したが、本発明のローリー出荷向け液化燃料ガスの成分調整装置はこれに限定されるものではなく、分離ガスを第一気液混合装置４７に供給しない態様も含む。この場合、分離ガスは例えばガス燃焼ボイラなどガスの熱量の制約が緩やかな機器に供給するようする。 Further, in the third and fourth embodiments, an example in which the separated gas separated by the gas-liquid separating device 49 is supplied to the first gas-liquid mixing device 47 of the liquefied fuel gas line 7 is shown. The component adjusting device for the liquefied fuel gas for lorry shipment is not limited to this, and includes a mode in which the separated gas is not supplied to the first gas-liquid mixing device 47. In this case, the separated gas is supplied to a device such as a gas combustion boiler in which the calorific value of the gas is loosely restricted.

１成分調整装置
３ＬＮＧタンク
５ＬＮＧ送出ポンプ
７液化燃料ガスライン
９第一ライン
１１ローリー
１３第二ライン
１５昇圧ポンプ
１７気化器
１９膜分離装置
２１気液混合装置
２３ローリータンク
２５減圧装置
２７濃縮ガス供給ライン
２９リターンガスライン
３１濃縮ガス制御弁
３３制御装置
３５演算部
３７制御部
３９成分調整装置（実施の形態２）
４１熱交換器
４３成分調整装置（実施の形態３）
４５濃縮ガス分離供給ライン
４７第一気液混合装置
４９気液分離装置
５１分離液供給ライン
５３分離ガス供給ライン
５５分離液制御弁
５７分離ガス制御弁
５９第２の制御装置
６１第２演算部
６３第２制御部
６５成分調整装置（実施の形態４）
６７ＬＮＧ供給ライン
６９ＬＮＧ制御弁
７１第３の制御装置
７３第３演算部
７５第３制御部 1 Component adjustment device 3 LNG tank 5 LNG delivery pump 7 Liquefied fuel gas line 9 1st line 11 Raleigh 13 2nd line 15 Booster pump 17 Vaporizer 19 Membrane separator 21 Gas-liquid mixing device 23 Raleigh tank 25 Decompression device 27 Concentrated gas Supply line 29 Return gas line 31 Concentrated gas control valve 33 Control device 35 Calculation unit 37 Control unit 39 Component adjustment device (Embodiment 2)
41 Heat exchanger 43 Component adjusting device (Embodiment 3)
45 Concentrated gas separation supply line 47 First gas-liquid mixer 49 Gas-liquid separation device 51 Separation liquid supply line 53 Separation gas supply line 55 Separation liquid control valve 57 Separation gas control valve 59 Second control device 61 Second calculation unit 63 Second Control Unit 65 Component Adjusting Device (Embodiment 4)
67 LNG supply line 69 LNG control valve 71 Third control device 73 Third calculation unit 75 Third control unit

Claims

A liquefied fuel gas line through which the liquefied fuel gas sent from the liquefied fuel tank flows, and a first line for supplying a low calorific value gas in which heavy components are diluted, which is a branch of the liquefied fuel gas line, and a heavy weight. Equipped with a second line for supplying high calorific value liquefied fuel gas with concentrated quality components to the lorry tank mounted on the lorry.
The first line has a booster pump for boosting the liquefied fuel gas, a vaporizer for vaporizing the boosted liquefied fuel gas, and a membrane separator for separating heavy components from the vaporized gas.
The second line includes a gas-liquid mixing device that mixes a concentrated gas in which a heavy component separated by the membrane separation device is concentrated with the liquefied fuel gas, and a mixed solution mixed by the gas-liquid mixing device. It has a decompression device that depressurizes the pressure below the withstand voltage of the lorry tank.
It is provided with a concentrated gas supply line for supplying the concentrated gas in which the heavy components separated by the membrane separation device are concentrated to the gas-liquid mixing device .
A heat exchanger is provided on the downstream side of the booster pump in the first line, and the concentrated gas flowing through the concentrated gas supply line is cooled by the heat exchanger with the cold heat of the liquefied fuel gas flowing through the first line. A component adjusting device for liquefied fuel gas for lorry shipment, which is characterized by being supplied to a liquid mixing device.

A liquefied fuel gas line through which the liquefied fuel gas sent from the liquefied fuel tank flows, and a first line for supplying a low calorific value gas in which heavy components are diluted, which is a branch of the liquefied fuel gas line, and a heavy weight. Equipped with a second line for supplying high calorific value liquefied fuel gas with concentrated quality components to the lorry tank mounted on the lorry.
The first line has a booster pump for boosting the liquefied fuel gas, a vaporizer for vaporizing the boosted liquefied fuel gas, and a membrane separator for separating heavy components from the vaporized gas.
The second line includes a gas-liquid mixing device that mixes a concentrated gas in which a heavy component separated by the membrane separation device is concentrated with the liquefied fuel gas, and a mixed solution mixed by the gas-liquid mixing device. It has a decompression device that depressurizes the pressure below the withstand voltage of the lorry tank.
A concentrated gas supply line that supplies a concentrated gas in which the heavy components separated by the membrane separation device are concentrated to the gas-liquid mixer, and a concentrated gas supply line .
A concentrated gas control valve provided in the concentrated gas supply line and adjusting the amount of concentrated gas flowing through the concentrated gas supply line.
A control device for controlling the concentrated gas control valve so that the calorific value of the liquefied fuel gas in the lorry tank does not exceed a predetermined calorific value is provided .
The control device is based on the pressure, temperature, flow rate and composition of the liquefied fuel gas supplied to the gas-liquid mixing device and the pressure, temperature, flow rate and composition of the concentrated gas flowing through the concentrated gas supply line. A liquefied fuel gas for lorry shipment, which further has a function of controlling the concentrated gas control valve so that the entire amount of the concentrated gas supplied to the gas-liquid mixing device is liquefied by the gas-liquid mixing device. Ingredient adjustment device.

A liquefied fuel gas line through which the liquefied fuel gas sent from the liquefied fuel tank flows, and a first line for supplying a low calorific value gas in which heavy components are diluted, which is a branch of the liquefied fuel gas line, and a heavy weight. Equipped with a second line for supplying high calorific value liquefied fuel gas with concentrated quality components to the lorry tank mounted on the lorry.
The first line has a booster pump for boosting the liquefied fuel gas, a vaporizer for vaporizing the boosted liquefied fuel gas, and a membrane separator for separating heavy components from the vaporized gas.
In the second line, a gas-liquid mixing device that mixes a concentrated gas in which a heavy component separated by the membrane separating device is concentrated with the liquefied fuel gas, and a mixed solution mixed by the gas-liquid mixing device are described. It has a decompression device that depressurizes the pressure below the withstand voltage of the lorry tank.
A concentrated gas supply line that supplies a concentrated gas in which the heavy components separated by the membrane separation device are concentrated to the gas-liquid mixing device, and a concentrated gas supply line .
A concentrated gas control valve provided in the concentrated gas supply line and adjusting the amount of concentrated gas flowing through the concentrated gas supply line.
A control device for controlling the concentrated gas control valve so that the calorific value of the liquefied fuel gas in the lorry tank does not exceed a predetermined calorific value is provided .
The control device determines the phase state of the mixed liquid based on the pressure, temperature and composition of the mixed liquid discharged from the gas-liquid mixing device on the downstream side of the gas-liquid mixing device, and the mixed liquid is a liquid. A component adjusting device for liquefied fuel gas for lorry shipment, which further has a function of controlling the concentrated gas control valve so as to be in a phase state.

A liquefied fuel gas line through which the liquefied fuel gas sent from the liquefied fuel tank flows, and a first line for supplying a low calorific value gas in which heavy components are diluted, which is a branch of the liquefied fuel gas line, and a heavy weight. The second line for supplying the high calorific value liquefied fuel gas with concentrated quality components to the lorry tank mounted on the lorry, and the concentrated gas with concentrated heavy components of the liquefied fuel gas flowing through the first line. It is provided with a concentrated gas separation supply line that separates gas and liquid with a gas and liquid separation device and supplies the separated separated liquid to the second line.
The first line has a booster pump that boosts the liquefied fuel, a vaporizer that vaporizes the boosted liquefied fuel gas, and a membrane separation device that separates heavy components from the vaporized gas.
The concentrated gas separation and supply line includes a concentrated gas supply line that supplies the concentrated gas separated by the membrane separation device to the gas-liquid separation device, and a liquefied fuel that is provided in the concentrated gas supply line and flows through the first line. It has a heat exchanger that cools the concentrated gas with the cold heat of the gas, and a separation liquid supply line that supplies the separation liquid separated by the gas-liquid separation device to the second line.
The second line is a component adjusting device for liquefied fuel gas for lorry shipment, which comprises a decompression device for reducing the pressure of the mixed liquid mixed with the separated liquid to a pressure equal to or lower than the pressure resistance of the lorry tank.

The concentrated gas separation supply line has a separation gas supply line that supplies the separation gas separated by the gas-liquid separation device to the first line.
The liquefied fuel for lorry shipment according to claim 4 , wherein the first line has a gas-liquid mixing device that mixes the separated gas with the liquefied fuel gas flowing through the first line on the upstream side of the booster pump. Gas component regulator.

Instead of providing a heat exchanger in the concentrated gas supply line, a liquefied fuel gas supply line is provided to supply a part of the liquefied fuel gas flowing through the first line from the downstream side of the booster pump to the gas-liquid separator. The component adjusting device for liquefied fuel gas for lorry shipment according to claim 4, wherein the component adjusting device is characterized.

Instead of providing a heat exchanger in the concentrated gas supply line, a liquefied fuel gas supply line is provided to supply a part of the liquefied fuel gas flowing through the first line from the downstream side of the booster pump to the gas-liquid separator. The component adjusting device for liquefied fuel gas for lorry shipment according to claim 5 , characterized in that.

A separation gas control valve provided in the separation gas supply line for adjusting the amount of separation gas supplied to the gas-liquid mixing device, and a concentration provided in the concentration gas supply line and supplied to the gas-liquid separation device. A concentrated gas control valve that adjusts the amount of gas, and a separation liquid control valve that is provided in the separation liquid supply line and adjusts the amount of the separation liquid supplied to the second line.
The pressure, temperature, flow rate and composition of the separation gas supplied to the separation gas supply line, the pressure, temperature, flow rate and composition of the liquefied fuel gas flowing through the first line, and the pressure in the gas-liquid separation device. The temperature and the liquid level are detected, respectively, and the separation gas control valve is controlled so that the total amount of the separation gas supplied to the gas-liquid mixing device is liquefied by the gas-liquid mixing device. Control to control the concentrated gas control valve and the separation liquid control valve so that the pressure and the liquid level of the above are within a predetermined range and the calorific value of the liquefied fuel gas in the lorry tank does not exceed a predetermined calorific value. The component adjusting device for liquefied fuel gas for lorry shipment according to claim 5, further comprising the device.

A separation gas control valve provided in the separation gas supply line to adjust the amount of separation gas supplied to the gas-liquid mixing device, and a concentration provided in the concentration gas supply line and supplied to the gas-liquid separation device. A concentrated gas control valve that adjusts the amount of gas, a liquefied fuel gas control valve that is provided in the liquefied fuel gas supply line and adjusts the amount of liquefied fuel gas supplied to the gas-liquid separation device, and the separation liquid supply line. A separation liquid control valve that is provided in the above and adjusts the amount of separation liquid supplied to the second line.
The pressure, temperature, flow rate and composition of the separation gas supplied to the separation gas supply line, the pressure, temperature, flow rate and composition of the liquefied fuel gas flowing through the first line, and the pressure in the gas-liquid separation device. The temperature and the liquid level are detected, respectively, and the separation gas control valve is controlled so that the total amount of the separation gas supplied to the gas-liquid mixing device is liquefied by the gas-liquid mixing device. The concentrated gas control valve, the liquefied fuel gas control valve, and the separation so that the pressure and the liquid level of the liquefied fuel gas in the lorry tank do not exceed a predetermined calorific value. The component adjusting device for liquefied fuel gas for lorry shipment according to claim 7, further comprising a control device for controlling a liquid control valve.