JP5984192B2 - Natural gas liquefaction process - Google Patents

Natural gas liquefaction process Download PDF

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JP5984192B2
JP5984192B2 JP2014515273A JP2014515273A JP5984192B2 JP 5984192 B2 JP5984192 B2 JP 5984192B2 JP 2014515273 A JP2014515273 A JP 2014515273A JP 2014515273 A JP2014515273 A JP 2014515273A JP 5984192 B2 JP5984192 B2 JP 5984192B2
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heat exchanger
gas
expander
natural gas
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JP2014522477A (en
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マウンダー，アンソニー，ドゥワイト
スキナー，ジェフリー，フレデリック
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0225—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers
    • F25J1/0227—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers within a refrigeration cascade
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
    • F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0235—Heat exchange integration
    • F25J1/0242—Waste heat recovery, e.g. from heat of compression
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
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    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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Description

本発明はメタンリッチガスの液化方法に関し、更に具体的には、但し排他的にではなく、液化天然ガス（ｌｉｑｕｅｆｉｅｄ ｎａｔｕｒａｌ ｇａｓ：ＬＮＧ）の製造方法に関する。   The present invention relates to a method for liquefying methane-rich gas, and more specifically, but not exclusively, to a method for producing liquefied natural gas (LNG).

天然ガスの液化は、実際には、
−液体冷媒の蒸発
−膨張機（エキスパンダー）におけるガスの仕事膨張
によって行うことができる。 The liquefaction of natural gas is actually
-Evaporation of liquid refrigerant-Can be performed by work expansion of gas in an expander.

液体冷媒の蒸発はその動力要求量が最低であるので、広く用いられているカスケードＬＮＧプロセス及び混合冷媒ＬＮＧプロセスの基礎になっている。   Since the evaporation of liquid refrigerant has the lowest power requirement, it is the basis for the widely used cascade LNG process and mixed refrigerant LNG process.

エキスパンダーに基づくＬＮＧ設備は、簡素であり、コンパクトであり、軽量であり、かつ、液体冷媒の購入／予備処理／貯蔵を避けることができる。これらの特性は、安全上の観点から炭化水素の在庫量を少なくしたい特にオフショアの小型の施設にとって魅力的である。しかし、エキスパンダープロセスはいくつかの欠点を有する。すなわち、
−近年までエキスパンダーの容量に制限があり、かつ経験が限られていること、
−動力要求量が高いこと、
−内部のガス流量が高いので、ラインの必要直径が大きくなること、
などである。 The expander-based LNG facility is simple, compact, lightweight, and avoids liquid refrigerant purchase / pretreatment / storage. These properties are particularly attractive for small offshore facilities that want to reduce hydrocarbon inventory from a safety standpoint. However, the expander process has several drawbacks. That is,
-Expander capacity is limited and experience is limited until recently,
-High power requirements,
-Because the internal gas flow rate is high, the required diameter of the line is increased,
Etc.

エキスパンダーに基づく殆どのプロセスについて、作業流体（通常窒素）はエキスパンダー出口において気相のままである。   For most processes based on expanders, the working fluid (usually nitrogen) remains in the gas phase at the expander outlet.

エキスパンダー内において原料ガスそのものが部分的に液化されて、２相の排出流れになると、その液化によって内部の（リサイクル）ガス流量が減少し、動力要求量が低減される。   When the raw material gas itself is partially liquefied in the expander to form a two-phase exhaust flow, the liquefaction reduces the internal (recycled) gas flow rate and reduces the power requirement.

液化エキスパンダーによるＬＮＧ製造は新規のアイディアではない（Ｂｏｃｑｕｅｔに付与された米国特許第２，９０３，８５８号明細書）。   LNG production with a liquefied expander is not a novel idea (US Pat. No. 2,903,858 to Bocquet).

本出願の発明者は、動力要求量を低くし得るプロセスを先に開示した（英国特許第２３９３５０４Ｂ号明細書及び米国特許第７，２３４，３２１号明細書）。このプロセスにおいては、液化エキスパンダーが、原料天然ガスから生成される単一の混合冷媒を含む予備冷却回路に接続される   The inventor of the present application has previously disclosed a process that can reduce power requirements (UK Patent 2393504B and US Pat. No. 7,234,321). In this process, a liquefied expander is connected to a precooling circuit containing a single mixed refrigerant generated from raw natural gas.

最近の他の文献は、並列／リサイクルガスエキスパンダーによって予備冷却し、これに液化エキスパンダーが後続する方式を開示している。例えば、
−国際公開第０１／４４７３５号パンフレット（Ｍｉｎｔａその他）は、「１６００ｐｓｉａより高い」圧力に圧縮された原料ガスからの−１１２℃の加圧液化天然ガス（ＰＬＮＧ）の製造を記載しており、
−米国特許出願公開第２００６／０２１３２２２号明細書（Ｗｈｉｔｅｓｅｌｌ）は、「約１５００ｐｓｉｇ〜約３５００ｐｓｉｇ」の圧力でプロセスに流入するか、あるいはプロセス内でその圧力に圧縮される原料ガスからのＬＮＧの製造を記載している。 Other recent publications disclose a method of pre-cooling with a parallel / recycle gas expander followed by a liquefied expander. For example,
-WO 01/44735 (Minta et al.) Describes the production of pressurized liquefied natural gas (PLNG) at -112 ° C from a source gas compressed to a pressure "higher than 1600 psia"
US 2006/0213222 (Whitesell) describes the production of LNG from a feed gas that flows into a process at a pressure of "about 1500 psig to about 3500 psig" or is compressed to that pressure within the process. Is described.

上記の２件の特許文献の内容に対して、本出願の進歩性は、約−１６１℃の大気圧ＬＮＧの実際の製造を可能にする２つのエキスパンダー（予備冷却エキスパンダー及び液化エキスパンダー）に対する運転条件を特定する点にある。更に、上記の特許文献における特徴である非常に高圧の原料ガスはもはや必要でない。   In contrast to the contents of the above two patent documents, the inventive step of the present application is based on operating conditions for two expanders (precooled expander and liquefied expander) that allow the actual production of atmospheric LNG at about -161 ° C. The point is to identify. Furthermore, the very high pressure source gas that is characteristic in the above-mentioned patent document is no longer necessary.

この結果、プロセスが簡素化され、熱効率が改善され、更に、原料ガスが４０ｂａｒ（４ＭＰａ）程度の低い圧力であっても適用可能な広範囲の適用可能性が実現される。   As a result, the process is simplified, the thermal efficiency is improved, and furthermore, a wide range of applicability that can be applied even when the source gas is at a low pressure of about 40 bar (4 MPa) is realized.

本発明は、そのフローの構成が簡単であること、動力消費が低いこと、及び、液体冷媒の貯蔵と使用とに依拠していないことのために、比較的小さいガス田、特にオフショアのガス田からのＬＮＧの製造を容易にする。液化プロセスそのものは、全体的に、例えば冷媒の予備処理用としてのプロセス処理塔を必要としない。プロセス処理塔は、このような運転条件の下では、運転を容易ならざるものにする可能性が高いのである。   The present invention has a relatively small gas field, particularly an offshore gas field, due to its simple flow configuration, low power consumption, and no reliance on storage and use of liquid refrigerant. Facilitates the production of LNG from The liquefaction process itself does not require a process tower, for example, for pretreatment of the refrigerant. The process tower is likely to make it difficult to operate under these operating conditions.

本発明によれば、天然ガスまたは他のメタンリッチガスの液化プロセスが提供される。一般的に４０ｂａｒ（４ＭＰａ）〜１００ｂａｒ（１０ＭＰａ）の圧力の原料ガスが、前記のエキスパンダーに基づくプラントの構成によって液化され、約１ｂａｒ（０．１ＭＰａ）／−１６１℃のＬＮＧ製品が生成される。このプロセスは次の工程、すなわち、
−最初のステップにおいて、第１熱交換器によって、かつ第１仕事エキスパンダー内において、原料ガス及びリサイクルガス（以下に述べる）を冷却する工程であって、その熱交換器は、−５０℃〜−８０℃、好ましくは−６０℃〜−７０℃の流出温度を有し、そのエキスパンダーは、前記熱交換器の流出温度より低い流出温度を有し、かつ、そのエキスパンダーの流出ストリームは、前記熱交換器の低温側流路において再加熱され、続いて、上記のリサイクルガスの一部を形成するために再圧縮される、工程と、
−前記第１熱交換器からの前記冷却された流出ストリームを、部分的に、その流出ストリームが本質的に凝縮される第２熱交換器の高温側流路内に通し、かつ部分的に、第２仕事エキスパンダー内に通す工程であって、その第２エキスパンダーは第２熱交換器の低温流出流体より低い流出温度を有し、その第２エキスパンダーの流出ストリームはかなりの量の液体（通常１０〜１５重量％）を含み、そのエキスパンダーの流出流体は蒸気留分と液体留分とに分離され、蒸気留分は前記第２及び第１熱交換器の低温側流路において再加熱され、続いて、再圧縮され、上記のリサイクルガスの一部としてプロセスの流入側に戻される、工程と、
−上記の分離された液体及び第２熱交換器の高温側流路から凝縮された液体（両者共通常約−１２０℃）の圧力をほぼ大気圧に低下させ、放出されたフラッシュガスを上記の熱交換器における別の低温側流路内において再加熱し、かつ、液体をＬＮＧ製品として使用するために取り出す工程と、
を含む。 In accordance with the present invention, a natural gas or other methane rich gas liquefaction process is provided. In general, a feed gas at a pressure of 40 bar (4 MPa) to 100 bar (10 MPa) is liquefied by a plant configuration based on the expander to produce an LNG product of about 1 bar (0.1 MPa) /-161 ° C. This process involves the following steps:
-In the first step, the raw material gas and the recycle gas (described below) are cooled by the first heat exchanger and in the first work expander, the heat exchanger being An effluent temperature of 80 ° C, preferably -60 ° C to -70 ° C, the expander has an effluent temperature lower than the effluent temperature of the heat exchanger, and the effluent stream of the expander Reheated in the cold side flow path of the vessel and subsequently recompressed to form part of the recycled gas,
Passing the cooled effluent stream from the first heat exchanger partly into the hot side flow path of the second heat exchanger in which the effluent stream is essentially condensed, and partly, Passing through a second work expander, the second expander having an effluent temperature lower than the cold effluent of the second heat exchanger, the effluent stream of the second expander being a substantial amount of liquid (usually 10 The expander effluent is separated into a vapor fraction and a liquid fraction, and the vapor fraction is reheated in the low temperature side channels of the second and first heat exchangers, followed by Re-compressed and returned to the inflow side of the process as part of the recycle gas,
-Reducing the pressure of the separated liquid and the liquid condensed from the high-temperature side passage of the second heat exchanger (both usually -120 ° C) to approximately atmospheric pressure, Reheating in another cold side flow path in the heat exchanger and removing the liquid for use as an LNG product;
including.

リサイクルガスの圧縮動力に対する最低の要求量が、機械的仕事の抜き取りを、第２エキスパンダーのほぼ出口において１０ｂａｒ（１ＭＰａ）を超える圧力範囲に集中させることから得られることが見出された。この利点は、２つのエキスパンダーからの流出圧力を約１０ｂａｒ（１ＭＰａ）に均等化できる点にあり、第１熱交換器を３流路構成に縮減できる。   It has been found that the minimum requirement for recycle gas compression power is obtained by concentrating the extraction of mechanical work at a pressure range in excess of 10 bar (1 MPa) at approximately the outlet of the second expander. This advantage is that the outflow pressure from the two expanders can be equalized to about 10 bar (1 MPa), and the first heat exchanger can be reduced to a three-channel configuration.

殆どの既存のＬＮＧ製造は、熱交換器内においてＬＮＧ製品を形成するように天然ガスを冷却しかつ凝縮させるために、液体の冷媒の蒸発に依拠しているが、本発明は、適度な動力要求量を備えた液化プロセスであって、必要な冷却の大部分が、原料ガスそのものの仕事膨張によって供給されるプロセスを含んでいる。従って、極低温用の液体冷媒、あるいは窒素のような他の二次作業流体は必要でない。この方法で、低い温度レベルにおいてエネルギーが抜き取られ、これによって、結果的に熱力学的な効率が改善される。その結果、前記仕事エキスパンダーからの低温ガスの再加熱によって冷却される熱交換器内の凝縮によって形成されるＬＮＧに加えて、ＬＮＧのかなりの部分が、直接、仕事抜き取りエキスパンダーにおいて形成される。   Although most existing LNG production relies on the evaporation of a liquid refrigerant to cool and condense natural gas to form an LNG product in a heat exchanger, the present invention provides a modest power A liquefaction process with the required amount, which includes a process in which most of the cooling required is supplied by work expansion of the raw material gas itself. Therefore, no cryogenic liquid refrigerant or other secondary working fluid such as nitrogen is required. In this way, energy is extracted at low temperature levels, thereby improving the thermodynamic efficiency. As a result, in addition to the LNG formed by condensation in the heat exchanger that is cooled by reheating the cold gas from the work expander, a significant portion of the LNG is formed directly in the work extraction expander.

次に、本発明を添付の図面を参照して説明する。   The present invention will now be described with reference to the attached figures.

図１は、本発明の一実施形態によるプロセスを示すフローシートである。FIG. 1 is a flow sheet illustrating a process according to one embodiment of the present invention. 図２は、本発明の別の実施形態によるプロセスを示すフローシートである。FIG. 2 is a flow sheet illustrating a process according to another embodiment of the present invention.

図１は本発明の基本的な運転上の特徴を示す。正確なフローシートは原料ガスの仕様に応じて変化するであろうが、一般的にこのフローシートの基本要素を含むであろう。圧力に言及する場合は、本明細書においては単位として「ｂａｒ」を用いるが、この「ｂａｒ」は絶対圧力である。   FIG. 1 illustrates the basic operational features of the present invention. The exact flow sheet will vary depending on the specifications of the feed gas, but will generally include the basic elements of this flow sheet. When referring to pressure, the term “bar” is used herein as a unit, but this “bar” is absolute pressure.

原料天然ガス（ストリーム１）は予備処理段階Ａを通して供給される。予備処理段階Ａにおいては、ＣＯ２、Ｈ２Ｓ、水蒸気及び水銀蒸気のような、固結するか、あるいは他の態様で下流側の液化プロセスと干渉する成分が、予備処理ガス（ストリーム２）における適切なかつ従来の最大の濃度になるのに必要な程度まで除去される。 Raw natural gas (stream 1) is fed through pretreatment stage A. In pretreatment stage A, components that consolidate or otherwise interfere with the downstream liquefaction process, such as CO 2 , H 2 S, water vapor and mercury vapor, are pretreated gas (stream 2). To the extent necessary to achieve a suitable and conventional maximum concentration.

ストリーム２はリサイクルガス（ストリーム３）の一部（ストリーム４）と混合され、ストリーム６を形成する。ストリーム６は、熱交換器Ｂの流路を通過し、通常−２０℃〜−６０℃の範囲、好ましくは−３０℃〜−５０℃の範囲の温度でストリーム７として流出する。この温度は、通常、最終のＬＮＧ製品用の仕様に適合するために、必要かつ十分なＮＧＬを凝縮するのに十分な程度に低い。セパレータＣにおいて凝縮されるあらゆる炭化水素がストリーム８として取り出される。Ｃからの流出蒸気（ストリーム９）は熱交換器Ｄ内の流路において更に冷却され、−５０℃〜−８０℃、好ましくは−６０℃〜−７０℃の範囲の温度においてストリーム１０として流出する。リサイクルガスの残余の部分（ストリーム５）はガスエキスパンダーＥにおいて冷却され、ストリーム１０の温度より低い温度の流出ストリーム１１として流出する。   Stream 2 is mixed with a portion of the recycled gas (stream 3) (stream 4) to form stream 6. The stream 6 passes through the flow path of the heat exchanger B, and flows out as the stream 7 at a temperature in the range of -20 ° C to -60 ° C, preferably in the range of -30 ° C to -50 ° C. This temperature is usually low enough to condense the necessary and sufficient NGL to meet the specifications for the final LNG product. Any hydrocarbons condensed in separator C are removed as stream 8. Outflow vapor from C (stream 9) is further cooled in the flow path in heat exchanger D and exits as stream 10 at a temperature in the range of -50 ° C to -80 ° C, preferably -60 ° C to -70 ° C. . The remaining portion of the recycle gas (stream 5) is cooled in the gas expander E and flows out as an effluent stream 11 having a temperature lower than that of the stream 10.

場合によっては、予備処理された原料ガスの一部またはすべてを、予備処理段階Ａからストリーム２ａを経由して流出させ、リサイクルガスのストリーム３がストリーム４及び５に分割される点の上流側でリサイクルガスのストリーム３に合流させることができる。この方式は、天然ガスの原料ストリーム１が僅少量の重質炭化水素しか含まない場合に有用であり得る。このような場合は、予備処理された原料ガスを全リサイクルガスと混合することができ、その結果得られた混合物を、続いて、ストリーム６としての熱交換器Ｂへの供給用と、ストリーム５としてのガスエキスパンダーＥへの供給用とに分割することができる。   In some cases, some or all of the pretreated source gas is discharged from pretreatment stage A via stream 2a upstream of the point where the recycled gas stream 3 is split into streams 4 and 5. Recycled gas stream 3 can be merged. This scheme may be useful when the natural gas feed stream 1 contains only a small amount of heavy hydrocarbons. In such a case, the pretreated source gas can be mixed with the total recycle gas, and the resulting mixture is subsequently fed to heat exchanger B as stream 6 and stream 5 The gas expander E can be divided into those for supply to the gas expander E.

ストリーム１１の圧力は、通常、約１５ｂａｒ（１．５ＭＰａ）となるであろう。ストリーム１１は熱交換器Ｄにおける第１低温側流路に流入し、ストリーム１２として流出する。ストリーム１２は、続いて熱交換器Ｂにおける第１低温側流路を通過し、ストリーム６の温度のすぐ下の温度で流出する（ストリーム１３）。ストリーム４の流量とストリーム５の流量との比率は、熱交換器Ｂ及びＤの合成した高温側及び低温側の間の温度の接近がそれらの全長にわたって一様になるように制御される。   The pressure in stream 11 will typically be about 15 bar (1.5 MPa). The stream 11 flows into the first low temperature side flow path in the heat exchanger D and flows out as the stream 12. The stream 12 subsequently passes through the first low temperature side flow path in the heat exchanger B and flows out at a temperature just below the temperature of the stream 6 (stream 13). The ratio of the flow rate of stream 4 to the flow rate of stream 5 is controlled so that the temperature approach between the combined hot and cold sides of heat exchangers B and D is uniform over their entire length.

ストリーム１０の大部分は、引き続いて、第２ガスエキスパンダーＦを通過し（ストリーム１４）、そのエキスパンダーＦから、３ｂａｒ（０．３ＭＰａ）〜２０ｂａｒ（２ＭＰａ）、好ましくは５ｂａｒ（０．５ＭＰａ）〜１５ｂａｒ（１．５ＭＰａ）の圧力で、かつ、部分的に液化された状態でストリーム１５として流出する。ストリーム１５は、続いて気液セパレータＧに流入する。セパレータＧからの液相部分（ストリーム１６）は、続いて、通常弁またはタービンのような減圧装置Ｈにおいて減圧される。Ｈからの流出分（ストリーム１７）は、通常大気圧かまたはそれに近い圧力であり、ＬＮＧタンクＩに送られる。製品ＬＮＧの窒素含有量を低減したい場合には、従来型の窒素ストリッピング塔（図示なし）を用いることができるが、この場合、通常、再沸用としてはストリーム１６の顕熱を利用する。   The majority of the stream 10 subsequently passes through the second gas expander F (stream 14) and from that expander F 3 bar (0.3 MPa) to 20 bar (2 MPa), preferably 5 bar (0.5 MPa) to 15 bar. It flows out as a stream 15 at a pressure of (1.5 MPa) and in a partially liquefied state. The stream 15 then flows into the gas / liquid separator G. The liquid phase portion (stream 16) from the separator G is subsequently depressurized in a decompressor H such as a normal valve or turbine. The outflow from H (stream 17) is usually at or near atmospheric pressure and is sent to LNG tank I. If it is desired to reduce the nitrogen content of the product LNG, a conventional nitrogen stripping tower (not shown) can be used. In this case, the sensible heat of the stream 16 is usually used for reboiling.

任意選択的なかつ好ましい方式として、ストリーム１０の一部が、ストリーム２３として熱交換器Ｊの高温側流路を通過し、その熱交換器Ｊにおいて、セパレータＧからの蒸気（ストリーム１８）との間接熱交換によって液化され、ストリーム２４として流出する。ストリーム２４は、続いて、通常弁またはタービンのような減圧装置Ｋによって減圧される。Ｋからの流出分は、ストリーム２５ａとして破線で示されるように気液セパレータＧに導かれるか、あるいは、好ましくは、ストリーム２５ｂとしてＬＮＧタンクＩに導かれる。この第２の選択方式は、リサイクルガス中の窒素の蓄積を低減するのに役立つ。ストリーム１８は、熱交換器Ｊの第１低温側流路において加熱されてストリーム１９として流出する。ストリーム１９は、続いて、熱交換器Ｄの第２低温側流路において更に加熱され、ストリーム２０として流出する。ストリーム２０は、続いて、熱交換器Ｂの第２低温側流路において更に加熱され、ストリーム６の温度より僅かに低い温度で、ストリーム２１として流出する。   As an optional and preferred scheme, a portion of stream 10 passes through the hot side flow path of heat exchanger J as stream 23 where indirect communication with steam from separator G (stream 18). It is liquefied by heat exchange and flows out as a stream 24. The stream 24 is subsequently depressurized by a decompressor K such as a normal valve or turbine. The outflow from K is led to the gas-liquid separator G as shown by the broken line as the stream 25a, or preferably, led to the LNG tank I as the stream 25b. This second selection scheme helps reduce the accumulation of nitrogen in the recycle gas. The stream 18 is heated in the first low temperature side flow path of the heat exchanger J and flows out as a stream 19. Subsequently, the stream 19 is further heated in the second low temperature side flow path of the heat exchanger D and flows out as a stream 20. Subsequently, the stream 20 is further heated in the second low temperature side flow path of the heat exchanger B, and flows out as a stream 21 at a temperature slightly lower than the temperature of the stream 6.

ストリーム１３及び２１はリサイクル圧縮機Ｎにおいて圧縮され、その圧縮機Ｎからの流出ストリーム３４は、通常、冷却器Ｏにおいて冷却水によって冷却される。圧縮機Ｎはインタクーラを備えた多段構成とすることができる。ストリーム１３及び２１は、同じ圧力ではないので、異なる圧縮機段に流入させることになるであろう。Ｏからの流出ストリームが、上記のリサイクルガスのストリーム３を形成する。   Streams 13 and 21 are compressed in recycle compressor N, and the effluent stream 34 from compressor N is typically cooled by cooling water in cooler O. The compressor N may have a multistage configuration including an intercooler. Streams 13 and 21 will not be at the same pressure and will therefore flow into different compressor stages. The effluent stream from O forms the recycle gas stream 3 described above.

Ｈを通してのストリーム１６のフラッシング及びＫを通してのストリーム２４のフラッシングによって、原料ガスの窒素含有量の殆どと共に主としてメタンを含む蒸気が発生するであろう。通常、この蒸気（ストリーム２６）は、任意選択的に、タンクＩ内への熱の漏入によって生じる蒸発蒸気と組み合わされて、熱交換器Ｊの第２低温側流路内で加熱され、ストリーム２７を形成する。ストリーム２７は、続いて、熱交換器Ｄの第３低温側流路内で加熱されてストリーム２８になり、最後に、熱交換器Ｂの第３低温側流路内で加熱されて、ストリーム６の温度より僅かに低い温度でストリーム２９として流出する。ストリーム２９の圧力が確実に大気圧以下に低下しないようにするため、ストリーム２６に、従来型のブースタブロワ（これも図示なし）を設けることができる。ストリーム２９は、通常燃料ガスとして用いることができる。   The flushing of stream 16 through H and the flushing of stream 24 through K will produce a vapor containing mainly methane with most of the nitrogen content of the feed gas. Typically, this steam (stream 26) is heated in the second cold side flow path of heat exchanger J, optionally in combination with the evaporating steam generated by the heat leak into tank I, and the stream 27 is formed. The stream 27 is subsequently heated in the third low temperature side flow path of the heat exchanger D to become a stream 28 and finally heated in the third low temperature side flow path of the heat exchanger B to be stream 6. It exits as stream 29 at a temperature slightly below the temperature of. In order to ensure that the pressure in stream 29 does not drop below atmospheric pressure, stream 26 can be provided with a conventional booster blower (also not shown). The stream 29 can be used as a normal fuel gas.

ストリーム２９の一部またはすべて（ストリーム３０）は、任意選択的に、リサイクルガスに戻すために低圧圧縮機Ｌにおいて圧縮することができる。これはストリーム３１として流出する。このストリーム３１は冷却器Ｍにおいて冷却され、その冷却器Ｍからの流出分（ストリーム３２）がストリーム２１に合流してストリーム２２を形成する。ストリーム２２は、続いて、この任意選択が用いられない場合の単独のストリーム２１の代わりに、リサイクル圧縮機Ｎの吸い込み側に流入する。別の任意選択として、リサイクルガス（ストリーム３３）を、通常ガスタービンの燃料用として、好適な点において圧縮機Ｎから引き抜く方式がある。ストリーム２９またはストリーム３３は、最終的に燃料として燃焼するのに先立って、予備処理段階Ａにおける吸着剤の再生用としてのストリッピングガスとして利用することが好都合である場合がある。   Part or all of stream 29 (stream 30) can optionally be compressed in low pressure compressor L for return to recycle gas. This flows out as stream 31. The stream 31 is cooled in the cooler M, and an outflow (stream 32) from the cooler M joins the stream 21 to form a stream 22. Stream 22 then flows into the suction side of recycle compressor N instead of a single stream 21 when this option is not used. Another option is to draw the recycle gas (stream 33) from the compressor N at a suitable point, usually for fuel in a gas turbine. Stream 29 or stream 33 may be advantageously used as a stripping gas for regeneration of the adsorbent in pretreatment stage A prior to final combustion as fuel.

図２は、本発明の別の好ましい実施形態を示すが、この実施形態においては、エキスパンダーＥ及びＦが、基本的に、３ｂａｒ（０．３ＭＰａ）〜２０ｂａｒ（２ＭＰａ）、好ましくは５ｂａｒ（０．５ＭＰａ）〜１５ｂａｒ（１．５ＭＰａ）の同じ流出圧力を有する。エキスパンダーＥからの流出ストリーム（ストリーム１１）は、続いて、ストリーム１９と結合され、ストリーム１９ａを形成する。ストリーム１９ａは図１のストリーム１９の位置で熱交換器Ｄに流入する。この場合、熱交換器Ｂ及びＤはただ３つの流路のみを有し、これによって、熱交換器の構造と、プラントの運転とが簡素化される。   FIG. 2 shows another preferred embodiment of the invention, in which the expanders E and F are basically from 3 bar (0.3 MPa) to 20 bar (2 MPa), preferably 5 bar (0. Having the same outflow pressure of 5 MPa) to 15 bar (1.5 MPa). The effluent stream (stream 11) from expander E is subsequently combined with stream 19 to form stream 19a. Stream 19a flows into heat exchanger D at the position of stream 19 in FIG. In this case, the heat exchangers B and D have only three flow paths, which simplifies the structure of the heat exchanger and the operation of the plant.

殆どの用途において、ストリーム２及び３は大気温度に近い温度を有するであろうことが予期されるが、この温度レベル以下に冷却することが有利である場合がある。これらのストリーム、及び、任意選択的に圧縮機のインタクーラ及びアフタクーラからの流出ストリームを、機械的な冷凍サイクルによって、あるいは、通常、臭化リチウム（ＬｉＢｒ）を用いる吸収式冷凍システムによって冷却することが可能である。臭化リチウムは、ガスタービン、ガスエンジンまたはコンバインドサイクル、あるいは他の何らかの適切な設備の排気ガスからの熱供給を受け取ることができる。   In most applications, it is expected that streams 2 and 3 will have a temperature close to ambient temperature, but it may be advantageous to cool below this temperature level. These streams, and optionally the effluent streams from the compressor intercoolers and aftercoolers, may be cooled by a mechanical refrigeration cycle or by an absorption refrigeration system, usually using lithium bromide (LiBr). Is possible. The lithium bromide can receive heat supply from the exhaust gas of a gas turbine, gas engine or combined cycle, or some other suitable facility.

Claims (8)

天然ガスまたは他のメタンリッチガスの液化プロセスであって、
−原料天然ガス（９）を、熱交換器（Ｄ）及び第１ガスエキスパンダー（Ｅ）によって、４０〜１００ｂａｒ（４〜１０ＭＰａ）の圧力において、−５０℃〜−８０℃の温度に冷却する工程であり、前記熱交換器は、前記原料天然ガス（９）を受け入れると共に、前記エキスパンダーの流出温度より高い流出温度を有する、工程と、
−前記エキスパンダーの流出ストリーム（１１）を、前記熱交換器（Ｄ）の第１低温側流路において、前記原料天然ガス（９）の前記熱交換器への流入温度のすぐ下の温度に再加熱し、圧縮し、かつリサイクルする工程と、
−前記熱交換器（Ｄ）からの低温流出ストリーム（１４）の一部またはすべてを、それが部分的に液化される第２エキスパンダー（Ｆ）内に通す工程と、
−前記第２エキスパンダー（Ｆ）の流出ストリーム（１５）を蒸気留分及び液体留分に分離する工程と、
−前記液体留分（１６）をＬＮＧ製品として使用するために捕集する工程と、
−前記蒸気留分（１９）を、前記熱交換器（Ｄ）の第２低温側流路において、前記原料天然ガス（９）の前記熱交換器への流入温度のすぐ下の温度に再加熱する工程と、
−前記再加熱された蒸気留分を、圧縮後、一部（５）は前記第１エキスパンダーに、一部（４）は前記熱交換器にリサイクルする工程と、
を含むプロセスにおいて、
前記第２エキスパンダー（Ｆ）の流出ストリーム（１５）の圧力が５〜１５ｂａｒ（０．５〜１．５ＭＰａ）である、
ことを特徴とするプロセス。 A liquefaction process of natural gas or other methane rich gas,
-The process of cooling raw material natural gas (9) to the temperature of -50 degreeC to -80 degreeC in the pressure of 40-100 bar (4-10 MPa) with a heat exchanger (D) and a 1st gas expander (E). The heat exchanger receives the raw natural gas (9) and has an outflow temperature higher than the outflow temperature of the expander;
The expander effluent stream (11) is re-introduced to a temperature just below the inflow temperature of the raw natural gas (9) into the heat exchanger in the first low temperature side flow path of the heat exchanger (D). Heating, compressing and recycling the process;
Passing part or all of the cold effluent stream (14) from the heat exchanger (D) into a second expander (F) where it is partially liquefied;
Separating the effluent stream (15) of the second expander (F) into a vapor fraction and a liquid fraction;
-Collecting said liquid fraction (16) for use as an LNG product;
-Reheating the steam fraction (19) to a temperature just below the inflow temperature of the raw material natural gas (9) into the heat exchanger in the second low temperature side channel of the heat exchanger (D); And a process of
-Recycling the reheated steam fraction after compression, part (5) into the first expander and part (4) into the heat exchanger;
In a process that includes
The pressure of the effluent stream (15) of the second expander (F) is 5 to 15 bar (0.5 to 1.5 MPa).
Process characterized by that. 請求項１に記載のプロセスにおいて、前記熱交換器が前記原料天然ガスのすべてを受け入れる、ことを特徴とするプロセス。   The process of claim 1, wherein the heat exchanger receives all of the raw natural gas. 請求項１に記載のプロセスにおいて、前記熱交換器が、前記原料天然ガスの少なくとも３０％を受け入れる、ことを特徴とするプロセス。 The process of claim 1, the process of the heat exchanger, accepting 30% even without less of the raw natural gas, characterized in that. 請求項１乃至３の何れか一項に記載のプロセスにおいて、前記原料天然ガスが−６０℃〜−７０℃の温度に冷却される、ことを特徴とするプロセス。   The process according to any one of claims 1 to 3, wherein the raw natural gas is cooled to a temperature of -60 ° C to -70 ° C. 請求項１乃至４の何れか一項に記載のプロセスの変形において、前記第１及び第２ガスエキスパンダー（Ｅ，Ｆ）が、５ｂａｒ（０．５ＭＰａ）〜１５ｂａｒ（１．５ＭＰａ）の基本的に同じ流出圧力を有し、その両エキスパンダーからの流出ストリーム（１９ａ）が、最終的な再加熱、圧縮及びリサイクルに先立って結合される、ことを特徴とするプロセス。   5. The process variant according to claim 1, wherein the first and second gas expanders (E, F) are basically between 5 bar (0.5 MPa) and 15 bar (1.5 MPa). Process characterized in that the effluent streams (19a) from both expanders having the same effluent pressure are combined prior to final reheating, compression and recycling. 請求項１乃至５の何れか一項に記載のプロセスにおいて、前記原料ストリーム及び／または圧縮機排出ストリーム及び／またはリサイクルストリームの任意の一部分またはすべてが、例えば臭化リチウム（ＬｉＢｒ）のような吸収式冷凍サイクルを用いて冷却される、ことを特徴とするプロセス。 Process according to any one of claims 1 to 5, wherein the feed stream and / or any portion or all of the compressor discharge stream and / or recycle streams, such as example if lithium bromide (LiBr) A process characterized by being cooled using an absorption refrigeration cycle. 請求項１乃至６の何れか一項に記載のプロセスにおいて、吸収式冷凍システムに必要な熱が、プロセスの圧縮機への動力供給用として用いることができるガスエンジンまたはタービンの排熱によって供給される、ことを特徴とするプロセス。   7. Process according to any one of the preceding claims, wherein the heat required for the absorption refrigeration system is supplied by exhaust heat from a gas engine or turbine that can be used to power the compressor of the process. A process characterized by that. 請求項１乃至７の何れか一項に記載のプロセスにおいて、原料ストリーム及び／またはリサイクルストリームの何れかの前記のような冷却が、原料ガスからの二酸化炭素及び／または他の不純物の除去と組み合わされる、ことを特徴とするプロセス。   8. Process according to any one of the preceding claims, wherein such cooling of any of the feed streams and / or recycle streams is combined with the removal of carbon dioxide and / or other impurities from the feed gas. A process characterized by
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