WO2018070039A1 - 天然ガス液化設備 - Google Patents
天然ガス液化設備 Download PDFInfo
- Publication number
- WO2018070039A1 WO2018070039A1 PCT/JP2016/080562 JP2016080562W WO2018070039A1 WO 2018070039 A1 WO2018070039 A1 WO 2018070039A1 JP 2016080562 W JP2016080562 W JP 2016080562W WO 2018070039 A1 WO2018070039 A1 WO 2018070039A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- liquefaction
- natural gas
- fuel gas
- pressure
- Prior art date
Links
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
Definitions
- the present invention relates to an equipment configuration suitable for a small natural gas liquefaction equipment.
- Natural gas (NG: Natural Gas) produced in gas wells is liquefied in a natural gas liquefaction facility (NG liquefaction facility) and then liquefied natural gas (LNG: Liquefied Natural Gas) via an LNG tanker or pipeline And shipped to the consumption area.
- NG Natural Gas
- LNG Liquefied Natural Gas
- the NG liquefaction equipment includes various pretreatment devices for removing impurities such as moisture contained in NG, liquefaction treatment devices for liquefying NG, and storage tanks (LNG tanks) for storing liquefied LNG. Etc. and ancillary equipment are provided.
- NG is cooled using a refrigerant, and the refrigerant gas evaporated by heat exchange with the NG undergoes a temperature drop due to compression or adiabatic expansion using the compressor, and is re-cooled to cool NG. Used.
- the NG liquefaction facility includes a generator for supplying electric power to an electric motor such as a pump and a power source for driving the above-described refrigerant gas compressor.
- These power sources are operated by burning fuel gas including boil-off gas (BOG) generated by vaporization of LNG in the LNG tank.
- BOG boil-off gas
- Patent Document 1 the applicant provides a gas engine in an LNG receiving facility that receives LNG transported by an LNG tanker, and operates the gas engine using BOG generated in the LNG tank. , Developing power generation technology.
- the NG liquefaction facility is different from the LNG receiving facility in the configuration of the fuel gas supply facility and the fuel consumption balance, and the technique described in Patent Document 1 cannot be applied as it is.
- the present invention has been made under such a background, and an object thereof is to provide a facility configuration suitable for a small-sized natural gas liquefaction facility.
- the natural gas liquefaction facility of the present invention includes a liquefaction processing apparatus that performs a process of liquefying natural gas, A storage tank for storing liquefied natural gas liquefied by the liquefaction processing apparatus; A boil-off gas line having a boil-off gas compression unit for increasing the pressure of the boil-off gas generated in the storage tank; A gas engine that burns fuel gas and drives a generator; A fuel gas line that is pressurized in the boil-off gas compression section and supplies a fuel gas containing boil-off gas discharged from the boil-off gas line to the gas engine; A refrigerant compression unit that is driven by the electric power generated by the generator and compresses the refrigerant gas that has cooled the natural gas by the liquefaction processing apparatus.
- the natural gas liquefaction facility may have the following characteristics.
- the natural gas processing capacity of the liquefaction processing apparatus is a value within the range of 100,000 to 1,000,000 tons / year.
- the pressure of the fuel gas supplied from the fuel gas line to the gas engine is a value within the range of 0.6 to 1.0 MPaG.
- the fuel gas further includes another combustion device using the fuel gas, and the pressure of the fuel gas supplied from the fuel gas line to the other combustion device is the same as the pressure of the fuel gas supplied to the gas engine. There is.
- (C) a dehumidifying device that is provided on the inlet side of the liquefaction processing device and removes moisture in the natural gas supplied to the liquefaction processing device, and natural gas before being processed by the dehumidifying device,
- the natural gas before being liquefied by the liquefaction treatment apparatus is used as the fuel gas.
- a return gas line for joining the return gas returned from the gas tanker with the boil-off gas of the liquefied natural gas storage tank, and a part of the fuel gas including the gas boosted by the boil-off gas compression unit in the liquefaction processing device A reprocessing gas that is extracted as a reprocessing gas for reprocessing and includes a reprocessing gas compression unit that compresses the reprocessing gas, and supplies the reprocessing gas pressurized by the reprocessing gas compression unit to the inlet side of the liquefaction processing device And having a line.
- An exhaust heat recovery unit that recovers exhaust heat of the exhaust gas exhausted from the gas engine is provided, and the exhaust heat recovery unit is configured to remove the acid gas contained in the natural gas before being liquefied by the liquefaction treatment apparatus.
- Supply a heat source to at least one reboiler.
- the present invention drives a generator using a gas engine when supplying electric power for use in a natural gas liquefaction facility.
- Gas engines do not need to compress fuel gas at a high pressure compared to gas turbines, and can be operated stably over a wide range of outside air temperatures and loads. It can be set as the apparatus structure suitable for the small-sized natural gas liquefaction installation.
- FIG. 1 shows a configuration example of a small-sized NG liquefaction facility provided with a natural gas (NG) liquefaction treatment device 12.
- the NG liquefaction facility of this example includes a liquefaction processing apparatus 12 having a processing capacity of, for example, 300,000 tons / year within a range of 100,000 to 1,000,000 tons / year.
- Natural gas (NG) transported from a well source is subjected to mercury removal or acid gas removal by a mercury removal device or acid gas removal device (not shown), and then dehumidification device 11 for TEG (Tri Ethylene). Glycol) is used to remove water.
- the mercury removing device, the acid gas removing device, and the dehumidifying device correspond to the pretreatment device provided in the NG liquefaction facility of this example.
- the liquefaction processing apparatus 12 is an electrode that liquefies and supercools NG by cooling a NG with a scrub column that removes heavy components contained in NG, and a mixed refrigerant that includes a plurality of refrigerant raw materials such as nitrogen, methane, ethane, and propane.
- MCHE Main Cryogenic Heat Exchanger
- a refrigerant compressor 121 composed of a compressor by compressing the mixed refrigerant gas vaporized by heat exchange, and an after-cooler that cools the mixed refrigerant compressed by the refrigerant compressor 121
- Equipment such as a cooler is provided.
- the liquefaction treatment device 12 is provided with each fractionation device (ethane fractionation device, propane fractionation device, butane fractionation device) for fractionating ethane, propane, and butane separated from the cooled NG.
- each fractionation device ethane fractionation device, propane fractionation device, butane fractionation device
- each fractionation device for fractionating ethane, propane, and butane separated from the cooled NG.
- individual devices and apparatuses such as a scrub column, MCHE, aftercooler, and each fractionating apparatus constituting the liquefaction processing apparatus 12 are individually shown. The description is omitted.
- the liquefied natural gas (LNG) obtained by liquefying and supercooling NG in the liquefaction processing device 12 is sent to the LNG tank 13 and stored.
- the LNG stored in the LNG tank 13 is fed by the LNG pump 131, loaded into the LNG tanker 50 via the payout line 51, and then shipped to the consumption area.
- the NG liquefaction facility having the above-described configuration includes a generator 41 that supplies electric power to an electric motor such as a motor 122 that drives the refrigerant compressor 121.
- a fuel gas including boil-off gas (BOG) generated in the LNG tank 13 is used, and the generator 41 is driven using the gas engine 4.
- the fuel gas containing BOG is also used in other combustion equipment other than the gas engine 4 as boiler fuel provided in the NG liquefaction facility or pilot burner fuel of the flare stack.
- the fuel gas supply facility will be described with reference to FIG.
- BOG mainly composed of nitrogen or methane is generated due to heat input from the outer wall or a change in the liquid level of the LNG.
- the BOG generated in the LNG tank 13 is extracted to the boil-off gas line 601 and sent to the BOG compression unit 211 driven by the motor 212 via the boil-off gas line 601.
- the BOG compression unit 211 boosts the BOG to, for example, 0.7 MPaG within the range of 0.6 to 1.0 MPaG.
- the BOG boosted by the BOG compression unit 211 is cooled by the cooling unit 22 such as an air fin cooler and sent to the knockout drum 3 for separating moisture.
- the cooling unit 22 is not limited to the air fin cooler, but may be configured to cool the BOG by other methods such as a water-cooled heat exchanger.
- the natural gas line 605 before dehumidification for supplying the natural gas before being processed by the dehumidifier 11 and the liquefaction processor 12 are used.
- the BOG boosted by the BOG compression unit 211, the NG before dehumidification supplied from the dehumidified exhaust gas line 605, and the NG supplied from the replenishment gas line 606 flow through the fuel gas line 602 and the knockout drum 3. They are mixed and supplied as fuel gas to combustion equipment such as the gas engine 4. From this viewpoint, the knockout drum 3 also has a function of mixing BOG and NG.
- NG before dehumidification is supplied from the natural gas line 605 before dehumidification, thereby ensuring adjustment of the pressure control valve 242 described later. Further, NG from the supply gas line 606 is supplied to adjust the pressure of the fuel gas.
- the NG liquefaction facility of this example uses the gas engine 4 to drive the generator 41.
- the gas engine 4 is a gas turbine (for example, the supply pressure of fuel gas is 3.0 MPaG). It is possible to operate using low-pressure fuel gas.
- the fuel gas whose pressure is adjusted to, for example, 0.7 MPaG within the range of 0.6 to 1.0 MPaG is supplied to the gas engine 4 and other combustion equipment.
- the replenishment gas line 606 is provided with a pressure control valve 242.
- the pressure control valve 242 is, for example, based on the pressure detection result by the pressure gauge 241 provided in the fuel gas line 603 on the outlet side of the knockout drum 3, and the detected pressure approaches a predetermined set pressure (0.7 MPaG in this example). As described above, the supply amount of NG (pressure adjustment NG) supplied via the replenishment gas line 606 is increased or decreased.
- the knockout drum 3 may be provided with a function of suppressing rapid heat fluctuation of the fuel gas.
- Moisture is separated by the knockout drum 3 and the mixed fuel gas is heated to a temperature equal to or higher than the dew point temperature by the heating unit 23 and then supplied to the gas engine 4 via the fuel gas line 604A. .
- the fuel gas having the same pressure as the fuel gas supplied to the gas engine 4 is supplied to the other combustion devices via the fuel gas line 604B branched from the fuel gas line 604A.
- the heating unit 23 is not limited to the case where the heating unit 23 is configured by a heat exchanger that heats the fuel gas with a heating medium as shown in FIG. 1, and the BOG is formed by other methods such as a heater equipped with a burner. It is good also as a structure heated.
- the gas engine 4 drives the generator 41 using the fuel gas supplied from the fuel gas supply facility described above.
- a gas engine 4 having an output of about 5 to 20 MW, including for backup, is required in the liquefaction facility.
- a plurality of units, for example, about 1 to 5 units are provided according to the amount of electric power.
- the electric power generated by the generator 41 is supplied to various electric power use devices in the NG liquefaction facility, such as the motors 122 and 212 that drive the refrigerant compression unit 121 and the BOG compression unit 211 described above.
- the exhaust heat after the fuel gas is burned by the gas engine 4 is recovered as steam or the like by the exhaust heat recovery unit 401.
- the recovered heat is obtained by using the above-described acidic gas removing device for removing the acidic gas contained in NG, a reboiler for heating the absorbing solution when the absorbing solution for the acidic gas is regenerated, and the liquefaction processing device 12.
- a reboiler provided in a fractionation column of each fractionator (ethane fractionator, propane fractionator, butane fractionator) that fractionates ethane, propane, and butane separated from NG It is supplied as a heat source for at least one reboiler selected from the reboiler group.
- the NG liquefaction facility In the NG liquefaction facility according to the present embodiment having the above-described configuration, when LNG is loaded from the LNG tank 13 to the LNG tanker 50, hydrocarbon gas is generated in the LNG tanker 50, and this hydrocarbon is generated.
- the gas is returned to the NG liquefaction facility as a return gas.
- the return gas merges with the BOG flowing through the boil-off gas line 601 via the return gas line 52.
- the amount of the return gas returned from the LNG tanker 50 may reach several times the amount of BOG generated in the LNG tank 13, but as described above, for example, in the range of 0.6 to 1.0 MPaG.
- the entire amount of the return gas may be absorbed and not clean.
- the NG liquefaction facility of this example includes reprocessing gas lines 541 and 542 for extracting surplus fuel gas due to the supply of return gas and returning it to the liquefaction processing apparatus 12 for reprocessing.
- the reprocessing gas lines 541 and 542 are provided with a reprocessing gas compression unit 531 driven by a motor 532 to increase the pressure of the reprocessed fuel gas (reprocessing gas) to the acceptance pressure of the liquefaction processing apparatus 12 and further perform the reprocessing. After cooling in the gas cooling unit 533, the gas is returned to the inlet side of the liquefaction processing apparatus 12.
- the operation of the NG liquefaction facility having the above-described configuration will be described. If the amount of BOG generated decreases due to a decrease in the outside air temperature or a change in the liquid level in the LNG tank 13, the amount of BOG supplied from the BOG compressor 211 to the fuel gas line 602 is reduced. Less. As a result, the pressure of the fuel gas detected by the pressure gauge 241 changes in a decreasing direction, so that the pressure adjustment valve 242 opens the opening so that the detected pressure is maintained at the pressure setting value described above. Is increased to increase the supply amount of NG from the makeup gas line 606.
- the supply amount of the fuel gas to the fuel gas line 603 side decreases, so that the pressure control valve 242 maintains the detected pressure in the pressure gauge 241 at the set pressure, so the supply amount of NG from the supply gas line 606 Increase. Furthermore, when the amount of fuel gas generated is in a shortage balance, acceptance of NG before dehumidification through the dehumidified exhaust gas line 605 may be started.
- the hydrocarbon gas generated in the LNG tanker 50 is returned through the return gas line 52 and merged with the BOG as the return gas.
- the supply amount of the fuel gas raw material (BOG and return gas mixed gas) from the BOG compression unit 211 side increases, and the detected pressure of the pressure gauge 241 changes in the increasing direction. Therefore, the pressure control valve 242 decreases the supply amount of the pressure adjustment NG that has been increased in advance with the extraction of the reprocessing gas, and adjusts the fuel gas supply balance according to the return gas reception amount. .
- the reprocessed gas returned to the liquefaction processing apparatus 12 is processed together with NG, liquefied again, and stored in the LNG tank 13.
- surplus fuel gas that cannot be absorbed by the fuel gas supply facility is reprocessed and recovered as LNG, so that the surplus fuel gas is combusted and discarded by flares, etc.
- the loss of LNG can be reduced.
- the reprocessing gas compression unit 531 and the reprocessing gas cooling unit 533 are stopped, and the reprocessing of the fuel gas in the liquefaction processing device 12 is completed. To do. As a result, the fuel gas generation balance in the fuel gas supply facility returns to the state before starting the LNG loading operation.
- each device in the fuel gas supply facility described above is performed by controlling a control end of the pressure control valve 242 and the like, and a DCS (Distributed Control System) that controls the entire NG liquefaction facility using these control ends. ) And the like.
- DCS Distributed Control System
- the NG liquefaction facility has the following effects.
- the generator 41 When supplying electric power to be used in the NG liquefaction facility, the generator 41 is driven using the gas engine 4.
- the generator 41 does not need to compress the fuel gas to a high pressure as compared with the gas turbine, and can be stably operated in a wide range of outside air temperature and load. It can be set as the apparatus structure suitable for the small natural gas liquefaction installation to be drive
- the method of reprocessing the return gas from the LNG tanker 50 by the liquefaction processing device 12 is to merge the return gas into the BOG of the boil-off gas line 601 and then extract the fuel gas from the fuel gas line 602.
- the present invention is not limited to the example shown in FIG. 1 in which the reprocessing gas is returned to the inlet side of the liquefaction processing apparatus 12.
- the return gas line 52 is provided with a reprocessing gas compression unit 531 and a reprocessing gas cooling unit 533, and the downstream end thereof is directly connected to the inlet side of the liquefaction processing apparatus 12, thereby reprocessing the return gas. Gas may be used.
- the position where the reprocessing gas is returned is not limited to the inlet of the liquefaction processing apparatus 12, but may be the inlet side of any pretreatment apparatus upstream of the liquefaction processing apparatus 12.
- impurities cury, acid gas, moisture
- FIG. 2 components having the same functions as those of the NG liquefaction facility described with reference to FIG. 1 are denoted by the same reference numerals as those used in FIG. 1.
- the greatest difference between the NG liquefaction facility according to the reference example (FIG. 2) is that the power source for driving the generator 72 and the refrigerant compressor 121. And a plurality of gas turbines 71 and 73 are provided. Unlike a small NG liquefaction facility, the installation of a pre-cooling heat exchanger is not omitted in a large NG liquefaction facility. Therefore, in addition to the refrigerant compressor 121 that compresses the mixed refrigerant, the pre-cooling refrigerant is compressed in the NG liquefaction facility. A refrigerant compressor 121 is provided.
- the gas turbines 71 and 73 need to be supplied with high-pressure fuel gas whose pressure is increased to 3.0 MPaG, for example.
- the BOG compressor 211 boosts the BOG to the pressure
- the pressure control valve 242 increases or decreases the supply amount of pressure adjustment NG so that the pressure detected by the pressure gauge 241 is maintained at the pressure.
- high pressure fuel gas is supplied to the gas turbines 71 and 73, and the fuel gas is burned to drive the generator 72 and the refrigerant compressor 121.
- the combustion exhaust heat of the gas turbines 71 and 73 is recovered as steam or the like by the exhaust heat recovery units 711 and 731.
- a pressure reducing valve 252 is provided in the fuel gas line 604B that supplies fuel gas to these combustion devices, and the high pressure fuel gas of 3.0 MPaG is decompressed to 0.7 MPaG, for example.
- the decompressed fuel gas is gas-liquid separated by the knockout drum 3 and then supplied to each combustion device via the low pressure fuel gas line 607 (low pressure fuel gas system).
- the NG liquefaction facility including the gas turbines 71 and 73 needs to be provided with two high-pressure / low-pressure fuel gas supply facilities, and the gas engine 4 that can be operated only by the low-pressure fuel gas supply facility. It differs from NG liquefaction equipment provided with.
- the high-pressure fuel gas supply facility has a larger adjustment margin for fuel gas than the low-pressure fuel gas supply facility. For this reason, even if the entire amount of the return gas generated during the loading operation of the LNG into the LNG tanker 50 is received, the surplus fuel gas resulting from the reception of the return gas is adjusted in pressure from the supply gas line 606. By reducing the amount of NG received, it can be balanced with consumption. For this reason, it is not necessary to provide a facility for returning the surplus fuel gas and return gas to the inlet side of the liquefaction processing apparatus 12 for reprocessing. Also in this point of view, the large NG liquefaction facility is different in configuration from the small NG liquefaction facility that requires a facility for reprocessing the surplus fuel gas or the like as reprocessing gas when receiving the return gas.
- Reference numeral 12 Liquefaction treatment device 121: Refrigerant compression unit 13: liquefied natural gas (LNG) tank 211: boil-off gas (BOG) compression unit 4: gas engine 41: generator 601: boil-off gas lines 602, 603, 604A, 604B Fuel gas line 8 controller
Abstract
Description
液化処理装置においては、冷媒を用いてNGの冷却が行われ、NGとの熱交換により気化した冷媒ガスは、圧縮機を用いた圧縮や断熱膨張に伴う温度降下を経て、NGの冷却に再利用される。
しかしながらこのような小型のNG液化装設備に適した動力源の選択や、選択された動力源に適合した燃料ガスの供給設備の提案が十分に行われているとは言い難い状況である。
しかしながらNG液化設備は、燃料ガスの供給設備の構成や、燃料の消費バランスがLNGの受入設備とは異なり、特許文献1に記載の技術をそのまま適用することはできない。
前記液化処理装置にて液化された液化天然ガスを貯蔵する貯蔵タンクと、
前記貯蔵タンク内で発生したボイルオフガスを昇圧するためのボイルオフガス圧縮部を備えたボイルオフガスラインと、
燃料ガスを燃焼して発電機を駆動するガスエンジンと、
前記ボイルオフガス圧縮部にて昇圧され、前記ボイルオフガスラインから払い出されたボイルオフガス含む燃料ガスを前記ガスエンジンへ供給する燃料ガスラインと、
前記発電機にて発電された電力により駆動され、前記液化処理装置にて天然ガスを冷却した冷媒のガスを圧縮する冷媒圧縮部と、を備えることを特徴とする。
(a) 前記液化処理装置の天然ガスの処理能力が10~100万トン/年の範囲内の値であること。
(b) 前記燃料ガスラインからガスエンジンに供給される燃料ガスの圧力が0.6~1.0MPaGの範囲内の値であること。このとき、前記燃料ガスを利用する他の燃焼機器をさらに備え、前記燃料ガスラインから他の燃焼機器へ供給される燃料ガスの圧力が、前記ガスエンジンへ供給される燃料ガスの圧力と共通であること。
(c)前記液化処理装置の入口側に設けられ、当該液化処理装置に供給される天然ガス中の水分を除去する脱湿装置と、前記脱湿装置にて処理される前の天然ガスを、前記燃料ガスラインに供給する脱湿前天然ガスラインと、前記燃料ガス供給ラインの圧力を予め設定された圧力に維持するため、前記液化処理装置にて液化される前の天然ガスを前記燃料ガスラインに供給する圧力調整ガスラインと、を備えたこと。
(d)前記貯蔵タンク内の液化天然ガスを液化天然ガスタンカーへと払い出す払い出しラインと、前記払い出しラインからの液化天然ガスの払い出しに伴って前記液化天然ガスタンカーにて発生し、当該液化天然ガスタンカーから戻された戻りガスを液化天然ガス貯蔵タンクのボイルオフガスと合流させる戻りガスラインと、前記ボイルオフガス圧縮部にて昇圧されたガスを含む燃料ガスの一部を前記液化処理装置にて再処理するための再処理ガスとして抜き出し、さらに圧縮する再処理ガス圧縮部を備え、前記再処理ガス圧縮部にて昇圧された再処理ガスを前記液化処理装置の入口側へ供給する再処理ガスラインと、を備えたこと。
(e)前記ガスエンジンから排出される排ガスの排熱を回収する排熱回収部を備え、前記排熱回収部は、前記液化処理装置にて液化される前の天然ガスに含まれる酸性ガスを除去する酸性ガス除去装置のリボイラーと、前記液化処理装置にて天然ガスから分離されたエタン、プロパン、ブタンの分留を行う各分留装置に設けられたリボイラーと、からなるリボイラー群から選択された少なくとも一つのリボイラーに熱源を供給すること。
なお図示の便宜上、図1においては、冷媒圧縮部121を特記した点を除き、液化処理装置12を構成する各機器や装置(スクラブカラム、MCHE、アフタークーラーや各分留装置など)の個別の記載は省略してある。
また、BOGを含む燃料ガスは、NG液化設備内に設けられたボイラー燃料や、フレアスタックのパイロットバーナー燃料として、ガスエンジン4以外の他の燃焼機器でも利用される。以下、図1を参照しながら、当該燃料ガスの供給設備について説明する。
ここで既述のように、本例のNG液化設備はガスエンジン4を用いて発電機41を駆動しているところ、ガスエンジン4は、ガスタービン(例えば燃料ガスの供給圧力が3.0MPaG)と比べて低圧の燃料ガスを用いて運転することができる。本例では、燃料ガスの圧力は、0.6~1.0MPaGの範囲内の例えば0.7MPaGに調整された燃料ガスが、ガスエンジン4及びその他の燃焼機器に対して供給される。
発電機41にて発電された電力は、既述の冷媒圧縮部121やBOG圧縮部211を駆動するモーター122、212など、NG液化設備内の各種の電力使用機器に供給される。
はじめに、LNGの積み込み作業を開始する前に、通常は停止されている再処理ガス圧縮部531や再処理ガス冷却部533を稼働させ、再処理ガスライン541、542を介して液化処理装置12の入口側へ所定流量の燃料ガス(再処理ガス)を戻し、再処理を開始する。この結果、燃料ガスライン603側への燃料ガスの供給量が減少するので、圧力調節弁242は、圧力計241における検出圧力を設定圧力に維持するため、補給ガスライン606からのNGの供給量を増大させる。さらに燃料ガスの発生量が不足のバランスとなる場合には、脱湿排ガスライン605を介した脱湿前のNGの受け入れを開始してもよい。
図2において、図1を用いて説明したNG液化設備と共通の機能を有する構成要素には、図1で用いたものと共通の符号を付してある。
小型のNG液化設備と異なり、大型のNG液化設備では予冷熱交換器の設置は省略しないので、当該NG液化設備には、混合冷媒を圧縮する冷媒圧縮部121に加えて、予冷用冷媒を圧縮する冷媒圧縮部121が設けられる。
この点において、数台程度のガスエンジン4を用いて動力を供給可能な小型のNG液化設備は、ガスエンジン4の活用に適しているといえる。
このように、ガスタービン71、73を備えたNG液化設備は、高圧/低圧の2系統の燃料ガス供給設備を設ける必要がある点において、低圧の燃料ガス供給設備のみで運転可能なガスエンジン4を備えるNG液化設備と相違している。
このため、余剰となった燃料ガスや戻りガスを液化処理装置12の入口側に戻して再処理する設備は設ける必要がない。この観点においても、大型のNG液化設備は、戻りガスの受け入れの際に余剰となる燃料ガスなどを再処理ガスとして再処理する設備が必要な小型のNG液化設備とは構成が異なっている。
12 液化処理装置
121 冷媒圧縮部
13 液化天然ガス(LNG)タンク
211 ボイルオフガス(BOG)圧縮部
4 ガスエンジン
41 発電機
601 ボイルオフガスライン
602、603、604A、604B
燃料ガスライン
8 制御部
Claims (7)
- 天然ガスを液化する処理を行う液化処理装置と、
前記液化処理装置にて液化された液化天然ガスを貯蔵する貯蔵タンクと、
前記貯蔵タンク内で発生したボイルオフガスを昇圧するためのボイルオフガス圧縮部を備えたボイルオフガスラインと、
燃料ガスを燃焼して発電機を駆動するガスエンジンと、
前記ボイルオフガス圧縮部にて昇圧されたボイルオフガス含む燃料ガスを前記ガスエンジンへ供給する燃料ガスラインと、
前記発電機にて発電された電力により駆動され、前記液化処理装置にて天然ガスを冷却した冷媒のガスを圧縮する冷媒圧縮部と、を備えることを特徴とする天然ガス液化設備。 - 前記液化処理装置の天然ガスの処理能力が10~100万トン/年の範囲内の値であることを特徴とする請求項1に記載の天然ガス液化設備。
- 前記燃料ガスラインからガスエンジンに供給される燃料ガスの圧力が0.6~1.0MPaGの範囲内の値であることを特徴とする請求項1に記載の天然ガス液化設備。
- 前記燃料ガスを利用する他の燃焼機器をさらに備え、
前記燃料ガスラインから他の燃焼機器へ供給される燃料ガスの圧力が、前記ガスエンジンへ供給される燃料ガスの圧力と共通であることを特徴とする請求項3に記載の天然ガス液化設備。 - 前記液化処理装置の入口側に設けられ、当該液化処理装置に供給される天然ガス中の水分を除去する脱湿装置と、
前記脱湿装置にて処理される前の天然ガスを、前記燃料ガスラインに供給する脱湿前天然ガスラインと、
前記燃料ガス供給ラインの圧力を予め設定された圧力に維持するため、前記液化処理装置にて液化される前の天然ガスを前記燃料ガスラインに供給する圧力調整ガスラインと、を備えたことを特徴とする請求項1に記載の天然ガス液化設備。 - 前記貯蔵タンク内の液化天然ガスを液化天然ガスタンカーへと払い出す払い出しラインと、
前記払い出しラインからの液化天然ガスの払い出しに伴って前記液化天然ガスタンカーにて発生し、当該液化天然ガスタンカーから戻された戻りガスを液化天然ガス貯蔵タンクのボイルオフガスと合流させる戻りガスラインと、
前記ボイルオフガス圧縮部にて昇圧されたガスを含む燃料ガスの一部を前記液化処理装置にて再処理するための再処理ガスとして抜き出し、さらに圧縮する再処理ガス圧縮部を備え、前記再処理ガス圧縮部にて昇圧された再処理ガスを前記液化処理装置の入口側へ供給する再処理ガスラインと、を備えたことを特徴とする請求項1に記載の天然ガス液化設備。 - 前記ガスエンジンから排出される排ガスの排熱を回収する排熱回収部を備え、前記排熱回収部は、前記液化処理装置にて液化される前の天然ガスに含まれる酸性ガスを除去する酸性ガス除去装置のリボイラーと、前記液化処理装置にて天然ガスから分離されたエタン、プロパン、ブタンの分留を行う各分留装置に設けられたリボイラーと、からなるリボイラー群から選択された少なくとも一つのリボイラーに熱源を供給することを特徴とする請求項1に記載の天然ガス液化設備。
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2016426102A AU2016426102B2 (en) | 2016-10-14 | 2016-10-14 | Natural gas liquefaction apparatus |
PCT/JP2016/080562 WO2018070039A1 (ja) | 2016-10-14 | 2016-10-14 | 天然ガス液化設備 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/JP2016/080562 WO2018070039A1 (ja) | 2016-10-14 | 2016-10-14 | 天然ガス液化設備 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2018070039A1 true WO2018070039A1 (ja) | 2018-04-19 |
Family
ID=61905261
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2016/080562 WO2018070039A1 (ja) | 2016-10-14 | 2016-10-14 | 天然ガス液化設備 |
Country Status (2)
Country | Link |
---|---|
AU (1) | AU2016426102B2 (ja) |
WO (1) | WO2018070039A1 (ja) |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2006526724A (ja) * | 2003-06-05 | 2006-11-24 | フルオー・テクノロジーズ・コーポレイシヨン | 液化天然ガスの再ガス化によるパワーサイクル |
JP2013087911A (ja) * | 2011-10-20 | 2013-05-13 | Mitsubishi Heavy Ind Ltd | 貯蔵槽の圧力上昇抑制装置、これを備えた圧力上昇抑制システム、この抑制方法、これを備えた液化ガス運搬船およびこれを備えた液化ガス貯蔵設備 |
JP2014031829A (ja) * | 2012-08-03 | 2014-02-20 | Chugoku Electric Power Co Inc:The | 残留lng回収方法 |
JP2016105022A (ja) * | 2016-03-01 | 2016-06-09 | 日揮株式会社 | 液化天然ガスの受入設備 |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3331214A (en) * | 1965-03-22 | 1967-07-18 | Conch Int Methane Ltd | Method for liquefying and storing natural gas and controlling the b.t.u. content |
US5568737A (en) * | 1994-11-10 | 1996-10-29 | Elcor Corporation | Hydrocarbon gas processing |
-
2016
- 2016-10-14 WO PCT/JP2016/080562 patent/WO2018070039A1/ja active Application Filing
- 2016-10-14 AU AU2016426102A patent/AU2016426102B2/en active Active
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP2006526724A (ja) * | 2003-06-05 | 2006-11-24 | フルオー・テクノロジーズ・コーポレイシヨン | 液化天然ガスの再ガス化によるパワーサイクル |
JP2013087911A (ja) * | 2011-10-20 | 2013-05-13 | Mitsubishi Heavy Ind Ltd | 貯蔵槽の圧力上昇抑制装置、これを備えた圧力上昇抑制システム、この抑制方法、これを備えた液化ガス運搬船およびこれを備えた液化ガス貯蔵設備 |
JP2014031829A (ja) * | 2012-08-03 | 2014-02-20 | Chugoku Electric Power Co Inc:The | 残留lng回収方法 |
JP2016105022A (ja) * | 2016-03-01 | 2016-06-09 | 日揮株式会社 | 液化天然ガスの受入設備 |
Also Published As
Publication number | Publication date |
---|---|
AU2016426102B2 (en) | 2023-02-23 |
AU2016426102A1 (en) | 2019-03-07 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
KR101788407B1 (ko) | 가스 처리 시스템 | |
KR101848139B1 (ko) | 가스 처리 시스템을 포함하는 선박 | |
US10378817B2 (en) | Flexible liquefied natural gas plant | |
JP6104926B2 (ja) | 発電システムおよび対応する方法 | |
KR102094587B1 (ko) | 보일 오프 가스 스트림 취급 방법 및 이를 위한 장치 | |
JP6158725B2 (ja) | ボイルオフガス回収システム | |
JP6250519B2 (ja) | ボイルオフガス回収システム | |
BR112019017533B1 (pt) | Sistema liquidificante de gás natural | |
WO2015128903A1 (ja) | 液化天然ガスの受入設備 | |
WO2018070039A1 (ja) | 天然ガス液化設備 | |
JP6429159B2 (ja) | ボイルオフガス回収システム | |
JP6341523B2 (ja) | ボイルオフガス回収システム | |
KR101503276B1 (ko) | 극지용 선박의 연료가스 공급 시스템 및 방법 | |
KR101824427B1 (ko) | 선박의 연료가스 공급시스템 | |
KR102433265B1 (ko) | 가스 처리 시스템 및 이를 포함하는 해양 부유물 | |
KR102433264B1 (ko) | 가스 처리 시스템 및 이를 포함하는 해양 부유물 | |
KR101805490B1 (ko) | Lng를 연료로 하는 선박 및 상기 선박의 개조 방법 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 16918555 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 2016426102 Country of ref document: AU Date of ref document: 20161014 Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 16918555 Country of ref document: EP Kind code of ref document: A1 |
|
NENP | Non-entry into the national phase |
Ref country code: JP |