JP5378681B2 - Treatment method of liquefied natural gas - Google Patents
Treatment method of liquefied natural gas Download PDFInfo
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- JP5378681B2 JP5378681B2 JP2007520826A JP2007520826A JP5378681B2 JP 5378681 B2 JP5378681 B2 JP 5378681B2 JP 2007520826 A JP2007520826 A JP 2007520826A JP 2007520826 A JP2007520826 A JP 2007520826A JP 5378681 B2 JP5378681 B2 JP 5378681B2
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- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
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- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
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- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
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- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
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Description
本発明は液化天然ガスの処理に関するものであり、特に沸点がメタンより低い成分を含有する液化天然ガスの処理に関する。このような成分の例は窒素である。明細書及び特許請求の範囲において「低沸点成分」や「沸点が低い成分」なる表現は、沸点がメタンより低い成分を示すのに用いられる。この処理法では、低沸点の成分の含有量を小さくした液化天然ガスを得るために液化天然ガスから低沸点成分を除去する。この改良された方法は2つのやり方、すなわち(1)従来の方法と同量の液化天然ガスを処理するか、又は(2)従来の方法より多くの量の液化天然ガスを処理するように適用できる。最初のやり方で適用される場合には、本発明の方法で処理される液化ガス中の低沸点成分の含有量は、従来の方法で処理される液化ガス中のものより少ない。二番目のやり方で適用される場合には、低沸点成分の含有量は維持され、液化ガスの量が増加する。 The present invention relates to processing of liquefied natural gas, and more particularly to processing of liquefied natural gas containing components having a boiling point lower than that of methane. An example of such a component is nitrogen. In the specification and claims, the expressions “low-boiling component” and “low-boiling component” are used to indicate a component having a boiling point lower than that of methane. In this treatment method, low-boiling components are removed from liquefied natural gas in order to obtain liquefied natural gas having a low content of low-boiling components. This improved method is applied in two ways: (1) treating the same amount of liquefied natural gas as the conventional method, or (2) treating a larger amount of liquefied natural gas than the conventional method. it can. When applied in the first way, the content of low-boiling components in the liquefied gas treated by the method of the present invention is less than that in the liquefied gas treated by the conventional method. When applied in the second way, the content of low-boiling components is maintained and the amount of liquefied gas is increased.
US-A-6199403には、窒素などの高揮発性成分をメタンの豊富な原料流から除去する方法が開示されている。US-A-6199403によると、膨張した液化天然ガス流が中間の高さ、すなわち単一の気液接触領域より低くないところにて分離塔に入る。 US-A-6199403 discloses a method for removing highly volatile components such as nitrogen from a methane-rich feed stream. According to US-A-6199403, the expanded liquefied natural gas stream enters the separation column at an intermediate height, i.e. not lower than a single gas-liquid contact area.
US-A-5421165は炭化水素の液化混合物の供給原料を脱窒素化する方法に関する。このためにUS-A-5421165では、複数の理論的分別ステージを含んだ脱窒素塔を用いる比較的複雑な方法が示唆されている。 US-A-542165 relates to a process for denitrifying a feedstock of a hydrocarbon liquefaction mixture. For this reason, U.S. Pat. No. 5,542,165 suggests a relatively complex method using a denitrification tower comprising a plurality of theoretical fractionation stages.
別の比較的複雑な方法が国際出願公開第WO02/50483号に記載されている。WO02/50483には、低沸点の成分を液化天然ガスから除去する方法がいくつか開示されている。WO02/50483によると、低沸点成分の含有量を減少させた液体生成物流が得られる。 Another relatively complex method is described in WO 02/50483. WO 02/50483 discloses several methods for removing low boiling components from liquefied natural gas. According to WO 02/50483, a liquid product stream with a reduced content of low-boiling components is obtained.
WO02/50483に記載の上記方法の問題点は、液体生成物流が望ましくない低沸点成分を多く含有していることである。
本発明の目的は上記問題を最小限に抑えることである。
本発明の別の目的は代わりの方法を提供することである。
本発明の更に別の目的は液化天然ガス流中の低沸点成分の量を減少させる簡単な方法を提供することである。
The object of the present invention is to minimize the above problems.
Another object of the present invention is to provide an alternative method.
Yet another object of the present invention is to provide a simple method for reducing the amount of low boiling components in a liquefied natural gas stream.
上記目的又はその他の目的の1つ又はそれ以上のものが、本発明に基づいて、
液化圧力にて供給され低沸点成分を含有した液化天然ガスを処理して低沸点成分の含有量の少ない液体生成物流を得る方法であって、
(a)前記液化ガスを分離圧力まで膨張させて膨張した二相流体を得る工程と;
(b)前記膨張した二相流体を単一の気液接触領域を備えた塔に、該塔内に配置された前記単一の気液接触領域より下方にて導入する工程と;
(c)前記二相流体から液体を前記塔の底に集めて前記塔の底から低沸点成分の含有量の少ない液体流を引き出して液体生成物流を得る工程と;
(d)前記二相流体から蒸気を前記単一の気液接触領域に対して貫流させる工程と;
(e)前記塔の最上部から低沸点成分の豊富なガス流を引き出す工程と;
(f)工程(c)で得られた前記ガス流を熱交換器において加熱して加熱ガス流を得る工程と;
(g)工程(f)で得られた前記加熱ガス流を燃料ガス圧力まで圧縮して燃料ガスを得る工程と;
(h)工程(g)で得られた前記燃料ガスから再循環流を分離する工程と;
(i)工程(h)で得られた前記再循環流を少なくとも部分的に凝縮して還流を得る工程と;
(j)工程(i)で得られた前記還流を分離圧力にて前記単一の気液接触領域より上方にて前記塔に導入する工程と;
を含む方法を提供することによって達成される。
One or more of the above or other purposes may be in accordance with the present invention,
A method of obtaining a liquid product stream having a low content of low-boiling components by treating liquefied natural gas supplied at a liquefying pressure and containing low-boiling components,
(A) expanding the liquefied gas to a separation pressure to obtain an expanded two-phase fluid;
(B) introducing the expanded two-phase fluid into a tower having a single gas-liquid contact area below the single gas-liquid contact area disposed in the tower;
(C) collecting a liquid from the two-phase fluid at the bottom of the column and drawing a liquid stream having a low content of low-boiling components from the bottom of the column to obtain a liquid product stream;
(D) flowing steam from the two-phase fluid through the single gas-liquid contact area;
(E) drawing a gas stream rich in low-boiling components from the top of the column;
(F) heating the gas stream obtained in step (c) in a heat exchanger to obtain a heated gas stream;
(G) compressing the heated gas stream obtained in step (f) to fuel gas pressure to obtain fuel gas;
(H) separating the recycle stream from the fuel gas obtained in step (g);
(I) at least partially condensing the recycle stream obtained in step (h) to obtain reflux;
(J) introducing the reflux obtained in step (i) into the tower at a separation pressure above the single gas-liquid contact area;
This is achieved by providing a method comprising:
出願人は本発明により得られた液体生成物流における低沸点成分の含有量が予想されるものよりも小さいことを見い出した。 Applicants have found that the content of low-boiling components in the liquid product stream obtained according to the present invention is lower than expected.
驚くべきことに、これらの望ましい結果は、本発明に基づいて工程(b)においてただ1つの気液接触領域を有する塔を用いる簡単な方法によって得られる。 Surprisingly, these desirable results are obtained according to the invention by a simple method using a column having only one gas-liquid contact area in step (b).
本発明による簡単な方法を用いることで、より費用効果の高いやり方で液体生成物流中の低沸点成分の量を減少させることができる。 By using a simple process according to the present invention, the amount of low boiling components in the liquid product stream can be reduced in a more cost effective manner.
また、本発明による方法は7モル%未満の低沸点成分を含んだ液化天然ガス流(液化圧力にて供給される)に対して特に適していることが分かった。
以下、例として添付の非限定的な図面に関して本発明を詳細に説明する。
It has also been found that the process according to the invention is particularly suitable for liquefied natural gas streams (supplied at the liquefaction pressure) containing less than 7 mol% of low-boiling components.
The invention will now be described in detail by way of example with reference to the accompanying non-limiting drawings.
図1を参照する。低沸点成分を含有した液化天然ガスが、導管1を介して膨張エンジン3の形式の膨張装置及び膨張エンジン3の排出導管6におけるジュール-トムソン弁5に液化圧力にて供給される。膨張装置では、液化ガスを分離圧力まで膨張させることができ、膨張した二相流体が得られる。この液化圧力は適切には3〜8.5MPaの範囲にあり、分離圧力は適切には0.1〜0.5MPaの範囲にある。 Please refer to FIG. Liquefied natural gas containing low-boiling components is supplied at liquefied pressure via conduit 1 to an expansion device in the form of expansion engine 3 and to Joule-Thomson valve 5 in discharge conduit 6 of expansion engine 3. In the expansion device, the liquefied gas can be expanded to the separation pressure, and an expanded two-phase fluid is obtained. This liquefaction pressure is suitably in the range of 3 to 8.5 MPa and the separation pressure is suitably in the range of 0.1 to 0.5 MPa.
膨張した二相流体は導管9を介して塔10に送られる。この膨張した二相流体はべーン入口装置12などの適当な入口装置を介して分離圧力にて塔10に導入される。schoepentoeter(商標)としても公知のべーン入口装置により、気体と液体の効率的な分離が可能になる。 The expanded two-phase fluid is sent to the tower 10 via the conduit 9. This expanded two-phase fluid is introduced into the tower 10 at a separation pressure via a suitable inlet device such as the vane inlet device 12. A vane inlet device, also known as schoepentoeter ™, allows efficient separation of gas and liquid.
この塔10はただ1つの気液接触領域14を備える。この単一接触領域14は、気体と液体を接触させる任意の適当な手段、例えばトレーやパッキングを備えることができる。好ましくは、この単一接触領域14は2〜8個の水平接触トレー15又は2〜8個の接触トレーに相当する長さの充填領域を有するパッキングから構成される。この膨張した二相流体は単一気液接触領域14より下にて塔10に導入される。 This tower 10 comprises only one gas-liquid contact area 14. This single contact area 14 may comprise any suitable means for contacting the gas and liquid, such as a tray or packing. Preferably, this single contact area 14 consists of a packing having a length of filling area corresponding to 2-8 horizontal contact trays 15 or 2-8 contact trays. This expanded two-phase fluid is introduced into the tower 10 below the single gas-liquid contact region 14.
塔10の底16では、二相流体から液体が集められ、低沸点成分の含有量の少ない液体流が底16から導管17を介して取り出されてポンプ18により貯蔵タンク20に送られる。貯蔵タンク20からは、液体生成物流が導管21を介して取り出され、ガス流が導管22を介して取り出される。このガス流はボイルオフ・ガスとしても知られている。 At the bottom 16 of the column 10, liquid is collected from the two-phase fluid, and a liquid stream having a low content of low boiling components is withdrawn from the bottom 16 via a conduit 17 and sent to a storage tank 20 by a pump 18. From the storage tank 20, a liquid product stream is withdrawn via conduit 21 and a gas stream is withdrawn via conduit 22. This gas stream is also known as boil-off gas.
二相流体から蒸気が単一接触領域14を貫流する。塔10の最上部23から低沸点成分の豊富なガス流が導管25を介して取り出される。このガス流は熱交換器27において加熱され、加熱して得られたガス流は導管28を介して圧縮機30に送られる。圧縮機30において、この加熱されたガス流が燃料ガス圧力まで圧縮されて燃料ガスを得る。この燃料ガスが導管31を介して取り出され、熱交換器32で冷却されて圧縮熱が取り除かれる。この燃料ガスが導管33を介して離れたところに送られる。この燃料ガスの圧力は1〜3.5MPaの範囲にある。 Steam from the two-phase fluid flows through the single contact region 14. A gas stream rich in low-boiling components is withdrawn from the top 23 of the column 10 via conduit 25. This gas stream is heated in the heat exchanger 27, and the gas stream obtained by heating is sent to the compressor 30 via the conduit 28. In the compressor 30, this heated gas stream is compressed to fuel gas pressure to obtain fuel gas. This fuel gas is taken out through the conduit 31 and cooled by the heat exchanger 32 to remove the compression heat. This fuel gas is sent to a remote location via a conduit 33. The pressure of this fuel gas is in the range of 1 to 3.5 MPa.
燃料ガスから再循環流が導管34aを介して熱交換器27に供給される。熱交換器27では、この再循環流が少なくとも部分的に凝縮されて還流を得て、この還流がジュール-トムソン弁37を備えた導管34bを介して塔10に送られる。この還流が分離圧力にて単一接触領域14より上方のべーン入口装置39などの入口装置を介して塔10に導入される。 A recirculation stream from the fuel gas is supplied to the heat exchanger 27 via a conduit 34a. In the heat exchanger 27, this recycle stream is at least partially condensed to obtain reflux, which is sent to the column 10 via a conduit 34 b equipped with a Joule-Thomson valve 37. This reflux is introduced at a separation pressure into the column 10 via an inlet device such as a vane inlet device 39 above the single contact region 14.
表1は仮想例の結果をまとめており、図1の方法と基準例を比較している。基準例では、再循環流と原料とが同じ高さにて塔に導入されているので、これらの2つの流れの液相が塔への導入の前に混合され、塔には接触領域がない。基準例において導管17から引き出された液体流は本発明における同じ流れよりも多くの窒素を含有することが分かった。 Table 1 summarizes the results of the hypothetical example, comparing the method of FIG. 1 with a reference example. In the reference example, the recycle stream and the feed are introduced into the tower at the same height, so the liquid phases of these two streams are mixed before introduction into the tower and the tower has no contact area. . It has been found that the liquid stream drawn from conduit 17 in the reference example contains more nitrogen than the same stream in the present invention.
表1は本発明の方法によって得られる生成物流中の窒素含有量がより少ないことを示している。 Table 1 shows that the nitrogen content in the product stream obtained by the process of the present invention is lower.
本発明の代替の態様では、燃料ガスから分離した再循環流を、それが熱交換器27で少なくとも部分的に凝縮される前に補助圧縮機において高圧に更に圧縮する。この高圧の再循環流はいくつかの方法で用いることができ、これについては図2に関して説明する。図1について既に説明した部分は同じ参照番号を有する。 In an alternative aspect of the invention, the recycle stream separated from the fuel gas is further compressed to high pressure in the auxiliary compressor before it is at least partially condensed in heat exchanger 27. This high pressure recirculation flow can be used in several ways, as will be described with respect to FIG. The parts already described with reference to FIG. 1 have the same reference numerals.
導管34a中に含まれるこの補助圧縮機は参照番号35により示される。この補助圧縮機35は冷却器(図示せず)を備えて圧縮された再循環流の圧縮熱を取り去ることができる。この圧縮された再循環流は熱交換器27において冷却することによって少なくとも部分的に凝縮される。必要とされる冷たさの一部は、導管25を介して送られる低沸点成分の豊富なガス流によって与えられる。残りは再循環流によって与えられる。再循環流からの冷たさは、再循環流の一部をジュール-トムソン弁38における中間圧力まで膨張し、膨張した流体を用いて導管34a中の再循環流を冷却し、この膨張した流体を導管38aを介して圧縮機30に供給することによって得ることができる。再循環流の一部を膨張させて得られるこの中間圧力は、圧縮機30の吸込圧力から排出圧力までの範囲にある(範囲の両端は含む)。この膨張した再循環流が圧縮機30に入るステージは、膨張した再循環流の圧力がそのステージにおける圧縮機30内の流体の圧力に一致するように選択される。 This auxiliary compressor contained in conduit 34a is indicated by reference numeral 35. The auxiliary compressor 35 includes a cooler (not shown) and can remove the compression heat of the compressed recirculation flow. This compressed recycle stream is at least partially condensed by cooling in heat exchanger 27. Part of the required coldness is provided by a low-boiling component rich gas stream sent via conduit 25. The rest is provided by the recirculation flow. The coolness from the recirculation flow expands a portion of the recirculation flow to an intermediate pressure at the Joule-Thomson valve 38, uses the expanded fluid to cool the recirculation flow in the conduit 34a, It can be obtained by feeding to the compressor 30 via the conduit 38a. This intermediate pressure obtained by expanding a part of the recirculation flow is in the range from the suction pressure to the discharge pressure of the compressor 30 (including both ends of the range). The stage where this expanded recirculation stream enters the compressor 30 is selected such that the pressure of the expanded recirculation stream matches the pressure of the fluid in the compressor 30 at that stage.
図1に関して説明したように、再循環流の残りはジュール-トムソン弁37により膨張させて還流として塔10に導入する。 As described with reference to FIG. 1, the remainder of the recirculation stream is expanded by Joule-Thomson valve 37 and introduced into column 10 as reflux.
図2に関して説明した態様の利点は、再循環流がより大きな圧力から膨張することで、より低い温度に冷却されることである。これにより、−145℃の原料流温度(上記の例)に比べてより温かい原料流、例えば−142℃の原料流が可能になる。よって、主低温熱交換器からの液化ガスの温度をより高くできるので、同量のエネルギーに対してより多くのガスを液化できる。 The advantage of the embodiment described with respect to FIG. 2 is that the recirculation stream is cooled to a lower temperature by expanding from a greater pressure. This allows for a warmer feed stream, eg, a -142 ° C. feed stream, compared to a -145 ° C. feed stream temperature (the example above). Therefore, since the temperature of the liquefied gas from the main low-temperature heat exchanger can be made higher, more gas can be liquefied for the same amount of energy.
補助圧縮機35から排出される流体の高圧は、補助圧縮機35を駆動するのに必要な動力の費用が、液化されるガスの増加量の値段よりも安くなるように選択される。 The high pressure of the fluid discharged from the auxiliary compressor 35 is selected such that the cost of power required to drive the auxiliary compressor 35 is less than the price of the increased amount of gas to be liquefied.
上記説明では、膨張弁37及び38において膨張が行われる態様を述べた。しかし、再循環流の膨張は2段階にて行なうことができ、すなわち最初はエキスパンダ36などの膨張装置にて行い、その後にジュール-トムソン弁37及び38にて行い得ることが分かる。 In the above description, the mode in which expansion is performed in the expansion valves 37 and 38 has been described. However, it can be seen that the recirculation flow can be expanded in two stages, i.e., initially with an expansion device such as expander 36 and then with Joule-Thomson valves 37 and 38.
膨張した流体を導管38aを介して圧縮機30に供給する代わりに、膨張した流体を圧縮機35の入口(図示せず)に供給することもできる。 Instead of supplying the expanded fluid to the compressor 30 via the conduit 38a, the expanded fluid can be supplied to the inlet (not shown) of the compressor 35.
図1及び2に関して説明した態様では、二相流体からの液体は塔10の底16に集められ、この底16から、低沸点成分の含有量の少ない液体流17が引き出されて液体生成物流を得る。本発明の代わりの態様では、この工程は、二相流体からの液体を塔の底に集めて低沸点成分の含有量の少ない液体流を塔の底を引き出し;この液体流を低圧にてフラッシュ容器に導入し;第2のガス流をフラッシュ容器の最上部から取り出し;そしてフラッシュ容器の底から液体流を取り出して液体生成物流を得る工程からなる。 In the embodiment described with respect to FIGS. 1 and 2, the liquid from the two-phase fluid is collected at the bottom 16 of the column 10, from which a liquid stream 17 with a low content of low boiling components is withdrawn to provide a liquid product stream. obtain. In an alternative embodiment of the present invention, this step collects liquid from the two-phase fluid at the bottom of the tower and draws a liquid stream with a low content of low boiling components to the bottom of the tower; this liquid stream is flushed at low pressure. Introducing the second gas stream from the top of the flash container; and removing the liquid stream from the bottom of the flash container to obtain a liquid product stream.
以下、この二容器の態様を図3に関して説明する。図1に関して既に説明した部分は同じ参照番号を有する。 Hereinafter, the embodiment of these two containers will be described with reference to FIG. Parts already described with respect to FIG. 1 have the same reference numerals.
塔10’は上部10uと下部10lとからなり、この上部は図1の塔10の機能を実行し、この下部10lは上部10uの圧力より低い圧力にて動作するフラッシュ容器である。適切には、上部10uの圧力は0.2〜0.5MPaの範囲にあり、フラッシュ容器10lの圧力は0.1〜0.2MPaの範囲にある。 The tower 10 'consists of an upper part 10u and a lower part 101, which performs the function of the tower 10 of FIG. 1, which is a flash vessel that operates at a pressure lower than the pressure of the upper part 10u. Suitably, the pressure in the upper part 10u is in the range of 0.2-0.5 MPa and the pressure in the flash vessel 10l is in the range of 0.1-0.2 MPa.
通常運転中、導管9を介して供給される二相流体からの液体が塔10’の上部10uの底16’に集められる。この底16’から、低沸点成分の含有量の少ない液体流が導管17’から引き出される。次に、この流れは低圧にてフラッシュ容器10lに導入される。この圧力低下は導管17’中のジュール-トムソン弁40によって得られる。その結果、二相混合物が形成され、入口装置41を介してフラッシュ容器10lに導入される。 During normal operation, liquid from the two-phase fluid supplied via conduit 9 is collected at the bottom 16 'of the top 10u of the column 10'. From this bottom 16 ', a liquid stream with a low content of low-boiling components is withdrawn from the conduit 17'. This stream is then introduced into the flash vessel 10l at low pressure. This pressure drop is obtained by Joule-Thomson valve 40 in conduit 17 '. As a result, a two-phase mixture is formed and introduced into the flash vessel 10l via the inlet device 41.
導管17”を介して、低沸点成分の含有量が少ない液体流が取り出されて貯蔵タンク20に送られる。 A liquid stream with a low content of low-boiling components is withdrawn via conduit 17 ″ and sent to storage tank 20.
フラッシュ容器10lの最上部23”から第2のガス流が取り出される。 A second gas stream is taken from the top 23 "of the flash vessel 10l.
適切には、この第2ガス流は導管42を介して熱交換器27に送られ、導管34aを介して供給される再循環流を用いた熱交換によってこの第2ガス流を加熱する。この加熱された流れは、圧縮機45で圧縮され、その圧縮熱は熱交換器48において除去されて導管49を介して送られ、この圧縮された第2ガス流が導管34aにおいて再循環流に加えられる。 Suitably, this second gas stream is sent via conduit 42 to heat exchanger 27, which heats this second gas stream by heat exchange using a recirculation stream supplied via conduit 34a. This heated stream is compressed in compressor 45, the heat of compression is removed in heat exchanger 48 and sent via conduit 49, and this compressed second gas stream is recirculated in conduit 34a. Added.
圧縮機45及び30は結合して1つの圧縮機(図示せず)にし得ることも分かる。この場合には、導管42はその圧縮機の吸込端部に連結され、導管28は中間入口に連結され、導管32はこの圧縮機の排出端部に連結される。 It can also be seen that the compressors 45 and 30 can be combined into a single compressor (not shown). In this case, conduit 42 is connected to the suction end of the compressor, conduit 28 is connected to the intermediate inlet, and conduit 32 is connected to the discharge end of the compressor.
本方法の利点は大型の液化プラントに使用できることである。 The advantage of this method is that it can be used in large liquefaction plants.
図1に関して説明した上記態様と同様に、図3に関して説明した態様もまた補助圧縮機を備えることができ、燃料ガスから分離した再循環流を熱交換器27において少なくとも部分的に凝縮する前に高圧に圧縮することができる。この高圧の再循環流はいくつかの方法にて用いることができ、これについては図4に関して説明する。図3に関して既に説明した部分は同じ参照番号を有する。 Similar to the embodiment described above with respect to FIG. 1, the embodiment described with respect to FIG. 3 can also include an auxiliary compressor, prior to at least partially condensing the recycle stream separated from the fuel gas in the heat exchanger 27. It can be compressed to high pressure. This high pressure recirculation flow can be used in several ways, as will be described with respect to FIG. Parts already described with respect to FIG. 3 have the same reference numerals.
導管34a中に含まれるこの補助圧縮機は参照番号35で示される。この補助圧縮機35は冷却器(図示せず)を備えて圧縮された再循環流の圧縮熱を取り去ることができる。この圧縮された再循環流はそれを熱交換器27において冷却することによって部分的に凝縮される。必要とされる冷たさの一部は、導管25を介して送られる低沸点成分の豊富なガス流によって与えられる。残りは再循環流によって与えられる。再循環流からの冷たさは、再循環流の一部をジュール-トムソン弁38において中間圧力まで膨張させ、膨張した流体を用いて導管34a中の再循環流を冷却し、この膨張した流体を導管38aを介して圧縮機30に供給することによって得ることができる。再循環流の一部を膨張して得られるこの中間圧力は、圧縮機30の吸込圧力から排出圧力までの範囲にある(範囲の両端は含まれる)。膨張した再循環流が圧縮機30に入る場所は、膨張した再循環流の圧力が当該入口の場所における圧縮機30内の流体の圧力に一致するように選択される。 This auxiliary compressor contained in conduit 34a is indicated by reference numeral 35. The auxiliary compressor 35 includes a cooler (not shown) and can remove the compression heat of the compressed recirculation flow. This compressed recycle stream is partially condensed by cooling it in heat exchanger 27. Part of the required coldness is provided by a low-boiling component rich gas stream sent via conduit 25. The rest is provided by the recirculation flow. The coolness from the recirculation flow causes a portion of the recirculation flow to expand to an intermediate pressure at the Joule-Thomson valve 38 and uses the expanded fluid to cool the recirculation flow in the conduit 34a, It can be obtained by feeding to the compressor 30 via the conduit 38a. This intermediate pressure obtained by expanding a part of the recirculation flow is in the range from the suction pressure to the discharge pressure of the compressor 30 (both ends of the range are included). The location where the expanded recirculation stream enters the compressor 30 is selected such that the pressure of the expanded recirculation flow matches the pressure of the fluid in the compressor 30 at the inlet location.
図1について説明したように、再循環流の残りはジュール-トムソン弁37により膨張させ、還流として塔10に導入する。 As described with reference to FIG. 1, the remainder of the recirculation stream is expanded by a Joule-Thomson valve 37 and introduced into the column 10 as reflux.
この態様の利点は、再循環流をより高い圧力から膨張させることで、より低い温度に冷却することである。これにより、−145℃の原料流温度(上記の例)に比べてより温かい原料流、例えば−142℃の原料流が許容される。よって、主低温熱交換器からの液化ガスの温度をより高くすることができるので、同量のエネルギーに対してより多くのガスを液化できる。 The advantage of this embodiment is that it is cooled to a lower temperature by expanding the recirculation stream from a higher pressure. This allows for a warmer feed stream, for example a -142 ° C. feed stream, compared to a feed stream temperature of −145 ° C. (above example). Therefore, since the temperature of the liquefied gas from the main low-temperature heat exchanger can be made higher, more gas can be liquefied for the same amount of energy.
補助圧縮機35から排出される流体の上記高圧は、補助圧縮機35を駆動するのに必要な動力の費用が、液化されるガスの増加量の値段よりも安くなるように選択される。 The high pressure of the fluid discharged from the auxiliary compressor 35 is selected such that the cost of power required to drive the auxiliary compressor 35 is lower than the price of the increased amount of gas to be liquefied.
上記説明では、膨張弁37及び38において膨張が行われる態様を説明した。しかし、再循環流の膨張は2段階にて、すなわち最初にエキスパンダ36などの膨張装置にて、その後にジュール-トムソン弁37及び38にて実行できることが分かる。 In the above description, the mode in which expansion is performed in the expansion valves 37 and 38 has been described. However, it can be seen that recirculation flow expansion can be performed in two stages, first with an expansion device such as expander 36 and then with Joule-Thomson valves 37 and 38.
図4はまた、貯蔵タンク20からのボイルオフ・ガスが導管22を介して圧縮機45の吸込端部に送られることを示している。 FIG. 4 also shows that boil-off gas from the storage tank 20 is sent via conduit 22 to the suction end of the compressor 45.
圧縮機45及び30を結合して1つの圧縮機(図示せず)にし得ることも分かる。その場合には、導管42(導管22が導管42中に開放している)がその圧縮機の吸込端部に連結され、導管28が中間入口に連結され、導管32が該圧縮機の排出端部に連結される。 It can also be seen that the compressors 45 and 30 can be combined into a single compressor (not shown). In that case, conduit 42 (conduit 22 open into conduit 42) is connected to the suction end of the compressor, conduit 28 is connected to the intermediate inlet, and conduit 32 is connected to the discharge end of the compressor. Connected to the part.
膨張した流体を導管38aを介して圧縮機30に供給する代わりに、圧縮機35の入口(図示せず)に供給することもできる。 Instead of supplying the expanded fluid to the compressor 30 via the conduit 38a, it may be supplied to the inlet (not shown) of the compressor 35.
図4の態様の代替案を図5に示す。図5では、導管34aを介して送られた再循環流の一部がそれから分離され、導管50を介して熱交換器27を通るように送られる。次に、この冷却された再循環流はエキスパンダ51において中間圧力に膨張され、導管34a中の再循環流を冷却するのに用いられる。次に、この膨張した流れは中間段階の圧縮機30に導入される。 An alternative to the embodiment of FIG. 4 is shown in FIG. In FIG. 5, a portion of the recycle stream sent via conduit 34a is separated therefrom and sent through heat exchanger 27 via conduit 50. This cooled recirculation stream is then expanded to an intermediate pressure in expander 51 and used to cool the recirculation stream in conduit 34a. This expanded stream is then introduced into an intermediate stage compressor 30.
適切には、導管34aを介して送られる再循環流は、導管31を介して送られる燃料ガスの10〜90質量%である。 Suitably, the recycle stream sent via conduit 34a is 10-90% by weight of the fuel gas sent via conduit 31.
図面に関して説明した態様では、単一接触領域14はトレーを備えているが、パッキングなどの他の任意の接触手段を用いることもできる。その場合、充填領域の長さは2〜8個の接触トレーに相当するようにするのが好ましい。 In the embodiment described with respect to the drawings, the single contact area 14 comprises a tray, but any other contact means such as packing could be used. In that case, it is preferred that the length of the filling area corresponds to 2 to 8 contact trays.
本発明の方法は液化天然ガス流中の低沸点成分の量を減少させる簡単な方法を提供する。 The method of the present invention provides a simple way to reduce the amount of low boiling components in the liquefied natural gas stream.
3 膨張エンジン
5 ジュール-トムソン弁
10 塔
12 べーン入口装置
14 気液接触領域
15 水平接触トレー
18 ポンプ
20 貯蔵タンク
30 圧縮機
27、32 熱交換器
3 Expansion Engine 5 Joule-Thomson Valve 10 Tower 12 Vane Inlet Device 14 Gas-Liquid Contact Area 15 Horizontal Contact Tray 18 Pump 20 Storage Tank 30 Compressor 27, 32 Heat Exchanger
Claims (5)
(a)前記液化ガスを分離圧力まで膨張させて膨張した二相流体を得る工程と;
(b)前記膨張した二相流体を単一の気液接触領域を備えた塔に、該塔内に配置された前記単一の気液接触領域より下方にて導入する工程と;
(c)前記二相流体から液体を前記塔の底に集めて前記塔の底から低沸点成分の含有量の少ない液体流を引き出して液体生成物流を得る工程と;
(d)前記二相流体から蒸気を前記単一の気液接触領域に対して貫流させる工程と;
(e)前記塔の最上部から低沸点成分の豊富なガス流を引き出す工程と;
(f)工程(e)で得られた前記ガス流を熱交換器において加熱して加熱ガス流を得る工程と;
(g)工程(f)で得られた前記加熱ガス流を燃料ガス圧力まで圧縮して燃料ガスを得る工程と;
(h)工程(g)で得られた前記燃料ガスから再循環流を分離する工程と;
(i)工程(h)で得られた前記再循環流を少なくとも部分的に凝縮して還流を得る工程と;
(j)工程(i)で得られた前記還流を分離圧力にて前記単一の気液接触領域より上方にて前記塔に導入する工程と;
を含む方法。 A method of obtaining a liquid product stream having a low content of low-boiling components by treating liquefied natural gas supplied at a liquefying pressure and containing low-boiling components,
(A) expanding the liquefied gas to a separation pressure to obtain an expanded two-phase fluid;
(B) introducing the expanded two-phase fluid into a tower having a single gas-liquid contact area below the single gas-liquid contact area disposed in the tower;
(C) collecting a liquid from the two-phase fluid at the bottom of the column and drawing a liquid stream having a low content of low-boiling components from the bottom of the column to obtain a liquid product stream;
(D) flowing steam from the two-phase fluid through the single gas-liquid contact area;
(E) drawing a gas stream rich in low-boiling components from the top of the column;
(F) heating the gas stream obtained in step ( e ) in a heat exchanger to obtain a heated gas stream;
(G) compressing the heated gas stream obtained in step (f) to fuel gas pressure to obtain fuel gas;
(H) separating the recycle stream from the fuel gas obtained in step (g);
(I) at least partially condensing the recycle stream obtained in step (h) to obtain reflux;
(J) introducing the reflux obtained in step (i) into the tower at a separation pressure above the single gas-liquid contact area;
Including methods.
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EP04254152 | 2004-07-12 | ||
EP04254152.4 | 2004-07-12 | ||
PCT/EP2005/053316 WO2006005746A1 (en) | 2004-07-12 | 2005-07-12 | Treating liquefied natural gas |
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US (2) | US20080066492A1 (en) |
EP (2) | EP1766311A1 (en) |
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MY140540A (en) | 2009-12-31 |
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JP5043655B2 (en) | 2012-10-10 |
KR20070034612A (en) | 2007-03-28 |
EP1766312A1 (en) | 2007-03-28 |
BRPI0512692A (en) | 2008-04-01 |
RU2007105107A (en) | 2008-08-20 |
JP2008506027A (en) | 2008-02-28 |
KR101238172B1 (en) | 2013-02-28 |
KR101178072B1 (en) | 2012-08-30 |
AU2005261729A1 (en) | 2006-01-19 |
RU2362954C2 (en) | 2009-07-27 |
AU2005261727B2 (en) | 2008-07-10 |
AU2005261727A1 (en) | 2006-01-19 |
KR20070032003A (en) | 2007-03-20 |
US20080066492A1 (en) | 2008-03-20 |
WO2006005746A1 (en) | 2006-01-19 |
BRPI0512693A (en) | 2008-04-01 |
PE20060219A1 (en) | 2006-05-03 |
EP1766311A1 (en) | 2007-03-28 |
PE20060221A1 (en) | 2006-05-03 |
US20080066493A1 (en) | 2008-03-20 |
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