TWI273207B - Dual stage nitrogen rejection from liquefied natural gas - Google Patents

Dual stage nitrogen rejection from liquefied natural gas Download PDF

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Publication number
TWI273207B
TWI273207B TW095114139A TW95114139A TWI273207B TW I273207 B TWI273207 B TW I273207B TW 095114139 A TW095114139 A TW 095114139A TW 95114139 A TW95114139 A TW 95114139A TW I273207 B TWI273207 B TW I273207B
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Taiwan
Prior art keywords
nitrogen
stream
natural gas
gas
liquefied natural
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TW095114139A
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English (en)
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TW200638013A (en
Inventor
Christopher Geoffrey Spilsbury
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Air Prod & Chem
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/028—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases
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    • F25J1/0015—Nitrogen
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column 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
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
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    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • 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
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Description

1273207 九、發明說明： - 發明所屬之技術領域 ，纟發明係、有關從液化天然氣（LNG)流移除氮氣。其對 於僅運用燃料氣體的部分氮氣同時將其餘的氮氣含量排放 至大氣有特別，但並非專門，的應用。所提供為分兩階段 在=濃度下移除氮氣的方法及用⑥天然氣液化以提供不 含氮氣的LNG產物的對應裝置。 •先前技術 • 燃氣渦輪（gas turbine)通常用於提供用於LNG設備的 軸功及電力。用於這些燃氣渦輪的燃料經常都以來自該 … LNG方法的廢氣的形式產生。在傳統的LNG方法中，存在 於該供料氣體中的氮氣正常都剔除至此燃料氣體中。然 而，用於這些渦輪之對於環境更友善的低一氧化氮（Ν〇χ) 燃燒器比先前所用的燃燒器對於該燃料氣體中的氮氣具有 參 更低的耐受性。因此，在某些含高氮氣含量的供料氣體之 設備位置，將從該LNG方法剔除比該燃氣渦輪燃料系統所 能接受更多的氮氣。 有數個先前技藝提議藉由分餾以較高濃度的物流從 LNG私除氮軋，其中使用冷凍或熱泵物流凝結來自該分餾 塔的塔頂蒸氣或提供迴流至該塔。 • US_A-2500118 (1950年3月7日核發）揭示一種天然氣 液化方法’其中在分離器中分離不純的LNG供料以提供 LNG底部物及氮氣塔頂物。使該氮氣塔頂物一部分凝結以 1273207 沒有從該分離 提供迴流至該分離器並且將其餘部分排掉 1§的LNG底部物進一步分離氮氣。 US_A_3205669 (1965 年 12月 14 曰枋々、姐 曰核發）揭示從天然氣 口收氣氣及氮氧。在第3圖的且濟々丨由 — J，、體例中，在「第二個」分 離器中將來自「第—個，分離哭、μ τ ^ ^ 弟個」刀雒益的不純LNG底部物分成塔 且在氮氣塔中分離其餘部分以提供底部液體及基本上純的 氮氣塔頂物。結合來自該第二個分離器的底部液體及該氮 氣塔並且蒸發以提供用於進一步加工的「殘餘氣體」。使來 自該第-個分離器的塔頂物冷卻並且供至氦氣分離器以提 頂蒸氣及底部液體。該塔頂物的一部分提供燃料氣體，並
供氮氣產物塔頂物及再循環物流。在改良的方法中，參照 第4及5圖來說明，刪除該氮氣塔，將來自該第二個分離 裔的塔頂物填至該氦氣分離器，並且由該氦氣分離器獲得 呈底部液體形態的氮氣。在另一個修飾例中，參照第6及 11/1 la圖來說明，保留該氮氣塔，但是供至第二個分離器 的供料係來自該氦氣分離器。在另外的修飾例中，表照第 7、8及1 〇圖來說明，刪除該氮氣塔，並且供至第二個分 離1§的供料係來自該氦氣分離器，藉以並未從該燃料氣體 分離氮氣。在所有的例示具體例中，該氦氣分離器的氮氣 含量都低於該第二個分離器的氮氣含量，若存在的話，該 第二個分離器的氮氣含量依序地低於該氮氣塔的氮氣含 。 US_A_3559417 (1971年2月2日核發）揭示，參照第玉 及2圖，在分餾塔中分離氮氣與LNG供料，提供呈液態底 1273207 部物的形態之純化LNG產物及氮氣塔頂物。該液態底部物 的一部分在該塔的頂部提供凝結作用但其組成沒有改變。 US-A-372 1099 (1965年12月14曰核發）揭示，參照第 圖天然氣的部分凝結，其中將預先冷卻的天然氣供料 成 弟 」蒸氣部分及「第一」LNG部分。進一步冷卻 該蒸氣部分並且分離以提供含有約2%氮氣的「第二」蒸氣 部分及含有約5%氮氣的「第二」LNG部分。在再沸器/凝 結器中凝結該第二蒸氣以提供再沸功能給雙精餾塔的較高 壓力（Γ HP」）塔。將凝結的混合物一部分供至該Hp塔，並 且使其餘部分與「第一」LNG部分一起再循環以提供冷凍 功能。該HP塔提供含有約95%氮氣的塔頂蒸氣及含有約 5%氮氣的底部液體。該塔頂物的—部分提供㈣功能給較 低壓力（「L P」）塔並且所得的凝結塔頂物提供迴流至該塔。 在該LP塔中分離該Hp塔底部液體及第二⑽部分以提 供約95%氮氣的塔頂蒸氣及約q.5%氮氣的⑽底部液 體’使其低溫冷卻並送去儲存。結合來自該Hp及Lp塔的 塔頂物並且用於提供冷凍功能。在修飾例中，沒有供至該 LP ί合的迴流並且來自該拔的叉 通合的塔頂瘵乳含有約20%氮氣並且 提供燃料氣體(第2圖)，而且視需要地，⑴將來自該Hp 塔再彿器/冷凝器的所有凝結蒸氣供至該册塔（第3圖）或 ⑻使所有預先冷卻的天然氣通過該抑塔再沸器/冷凝哭並 且供至該HP塔（第4圖）。 US-A-3874184 (1975 年 4 月 1 日核發）揭 儿 4丄 乂）褐不天然氣的液 化，/、中天然氣的局部液化所嫌媒沾 化所獲付的兩相物閃餾至分餾器 7 1273207 以提供富含氮氣的塔頂蒸氣及不純LNG底部物。以該塔了貝 物作為燃料氣體，並且閃餾該等底部物且供至分離器以提 ’供塔頂瘵氣及底部液體。該分餾器利用蒸發的底部液體再 /弗’並且利用低溫冷卻的底部液體使該分離器迴流。後繼 地閃餾該底部液體並且分離至兩個連續分離器内以提供 LNG產物。以來自這些分離器的塔頂物執行熱交換功能。 EP_A_0090469 (1983年10月5日核發；相當於 # 1^-八-4415345，1983年15日核發），揭示藉由冷卻並 且使用開迴路氮氣熱泵在低壓下分餾以產生用於分餾的液 . 體迴流而從氣態天然氣供料移除氮氣的方法。在單一塔具 • •體例中，僅對來自局部凝結的天然氣供料之蒸氣部分進行 分餾。藉由凝結該開迴路氮氣冷凍劑而提供用於該分餾塔 的再沸，並且藉由该减結的氮氣冷凍劑而提供用於該塔的 迴流。在例示的雙塔具體例中，該較高壓的塔靠局部凝結 的天然氣供料再沸，並且由該開迴路氮氣熱果來接受來自 # ㊉個塔的氮氣並提供再彿功能給壓力較低的塔並迴流至兩 個塔。該純化的LNG靠天然氣供料暖化並且以蒸氣的形態 回收。在該方法中並未製造出LNG最終產物。 EP-A一〇131128⑽5彳1月日公開；相當於 US A 45 042 95 19 85年3月12日核發）揭示使用可提供再 沸及迴流熱交換功能的閉迴路熱栗迴路，藉由局部凝結的 然氣的分顧將天然氣流分成氮氣流及甲烧氣流。在該方 • 法中並未製造出LNG最終產物。 XJS-A-4701200 fl987 ^ A _ 1 7年10月20日核發）揭示使用雙塔 !273207 氮氣剔除單元從天然氣分離氦氣，其中將Hp塔塔頂物分成 氣態富含氦氣部分及液態富含氮氣部分。進一步分離前者 以k供產物氦氣並且由後者提供迴流至該Hp及Lp技。在 λ LP i合中將该HP塔液悲底部物分成底部物及氮氣 塔頂蒸氣。供至該HP塔的天然氣供料係氣態。
w〇_A-93/08436 (1993年4月29日公開；相當於 US_A-5421 165，1995年6月6日核發）揭示藉由使lng冷 7並且在分餾之前以動態及靜態的方式膨脹而從lng物流 私除鼠氣。利用從該塔中間位置抽回的再沸物流並且返回 &中間位置下方的高度’至少局部地藉由熱交換而進行冷 口ρ。來自該分餾塔的塔頂蒸氣可予以壓縮並且作為燃料氣 體一部分壓縮的塔頂蒸氣可視需要地靠離開該塔的塔頂 :氣而局部地凝結，降低壓力並且以迴流的方式供至該 塔:一部分凝結的塔頂蒸氣可在輔助塔中分館以提供高純 度虱虱塔頂瘵氣及底部液體，使該底部液體減壓並且在供 /刀餾i合之别先與其餘部分結合。該辅助塔底部液體可 用於提供該輔助塔頂部分的凝結功能。 ^ EP_A_0725256 (1996年8月7日公開）揭示使氣態天然 礼^料冷部亚且分顧以移除氮氣的$法。#由冷卻該塔再 :^中的開迴路氮氣冷束劑而提供用於該分德塔的再沸蒸 《藉由功月》脹該冷卻的氮氣冷滚劑氣體以提供小量（4至 %)液+體而提供用於該塔頂部的迴流。至少—種來自該塔的 中間蒸氣流靠塔頂氮氣蒸氣流局部地凝結並且以中間迴流 的形式返回該塔，，亥中間迴流係供至該塔的迴流其中的大 9 1273207 4刀在日友化之4先將該天然氣注入至較高的壓力並且以 蒸氣產物的形式回收。在該方法中並未製造出lng .物。 、' GB_A-2298034 (1996年8月21日核發；相當於us冬 5617741，1997年4月8日核發）揭示使用具有主要塔及供 自並在如該主要塔之實質上相同壓力下操作的次要塔的雙 塔低溫蒸餾系統從天然氣供料流移除氮氣的方法。使來自 • 7主要塔的底部液體至少一部分在來自該塔的富含氮氣的 瘵氣熱交換過程中膨脹並且至少局部地蒸發，使該富含氮 ， 氣的蒸氣返回該主要塔以提供較高溫度的迴流。使來自該 …=要塔的底部液體在來自該等塔之一的塔頂蒸氣熱交換過 耘中至少局部蒸發以提供至少局部凝結的物流，使該至少 局部凝結的物流返回至該主要或次要塔以提供較低溫度的 迴流。藉由天然氣供料的熱交換提供再沸給該等塔。在此 方法中並未製造出LNG最終產物。 春 WO-A-0023164 (2000年4月27日核發；相當於 US_A_6199403，2〇〇1年3月13日核發）揭示在相分離器中 液化私脹然後分離天然氣流的方法，該相分離器可為氣 氣剔除塔。用於該塔的迴流可使用冷凍系統，藉由凝結一 部分塔頂蒸氣而提供。該冷凍系統可包含一閉迴路冷凍系 統·’ 一開迴路冷凍系統；及/或利用產物流的間接加熱交 換。負責凝結該塔頂蒸氣的熱交換器一部分可藉由抽自並 返回該塔的底部液流提供。該分離的LNG產物液體係注入 至較尚的壓力並且暖化。 10 1273207 US-A-6070429 (2_年6月6曰核發；相當於 W〇-A-005S674,2〇〇〇^10,
壓力下在串級的3個洗滌塔中分離由帶有加壓咖之物流 所獲得的加壓氣流以製造’㈣三個洗滌塔，富含氣氣的 氣流及富含甲烧的液流的方法，後面的物流適用於制環 至開放式甲烧循環液化方法及/或作為燃料氣體。在各自洗 務塔中’ I第-部分氣流的局部凝結所製得帶有液體的物 流以反向流舆該個別氣流的第二個部分接觸而提供塔頂蒸 氣及底部液體。該第一及第二個洗滌塔的塔頂蒸氣分別地 提供用於該第二及第三個洗滌塔的供料流。藉由來自該第 三個洗滌塔的塔頂蒸氣及底部液體提供供至該第二及第二 個洗滌塔的供料流之凝結功能。在例示的具體例中，將來 自該第二個洗滌塔的底部液體供至該第三個洗滌塔，而且 來自該第一個洗滌塔的底部液體可用於提供熱交換功能以 提供供至該第一個洗滌塔的局部凝結供料部分。 US-A-6449984 (2002 年 12 月 17 V 干u月17日核發；相當於 WO-A-03004951，2003 年 1 月 16 日公 P，、祖-，士 干1月10 H A開）揭不使天然氣流 液化然後分顧以提供富含氮氣的塔頂蒸氣及LNG底部液 體。藉由凝結一部分塔頂蒸氣而提供用於該分餾塔的迴 流。在例示的具體例中，該凝結功能係藉由冷凍劑流提供 並且與最終的LNG低溫冷卻熱交換器整合在一起。另外在 這些具體例中，從該分餾塔的中間位置抽取液體，靠供至 該塔的液化氣流供料來暖化並且返回該塔下方的位置。 WO-A-02088612 (2002年11月7日公開）揭示用於從 1273207 萄含烴的物流，特別是天然氣，移除氮氣的方法，其中在 液化的期間該局部凝結的物流係供至兩 /、 狄 ^ ^ ^ lu "合的虱氣剔除系 、、先。壓力較咼的塔提供富含氮氣的塔頂& ώΑ ^ ^ ^ …、乳该富含氮氣 的塔頂瘵氣靠來自該壓力較低的塔之挞 土 σ頂瘵虱凝結並以迴 ^的方式供至該壓力較低的塔。使來自壓 . 次！刀較两的塔之 底部液體冷卻並且供至該壓力較低的塔， 攸遇峻力較彳氏白勺 塔抽取液化產物作為底部液體。藉由供至該壓力較古的技 的局部凝結供料所提供的熱功能使該壓力較高的塔:滞 US 2003/0136146 (2003 年 7 月 24 日八 „ 乃μ曰公開；相當於 WO03062724，2003 年 7 月 31 日八 μ、祖- 、 千月31日么開）揭不用於製造LNG 及GTL (氣體變液體技術）的整合方法，其中在接續的閃基 罐中或其他分離器中分離LNG供料以提供個別的拔頂基氣 及逐漸純化的LNG底部物。以該分離器塔頂物作為燃料、 GTL原料或再循環物流。較佳為各自連續分離比前一個分 離更低至少15磅/平方吋（1巴）。 刀 US-A-2〇〇4231359 (2004 年 11 月 25 日公開；相當於 WO2004104143,2004 年 12 月 2 日八掘- 、 乃曰A開）揭不天然氣流液化 然後在蒸餾塔中分餾移除呈塔頂蒸氣產物形態的氮氣以及 呈底部液體形態的純化LNG的方法。藉由凝結的氮氣流提 供用於該塔的迴流。用以提供該迴流物流並冷卻該純化 LNG物抓及/或該液化天然氣供料的冷〉東作用係藉由壓縮 亚以功膨脹包含氮氣的冷凍劑物流而獲得，該氮氣包含來 自該:泰德塔的全部或一部分塔頂蒸氣。在例示的具體例 中，猎由供至該塔的液化天然氣供料提供用於再彿該分德 1273207 塔的熱交換功能。 WO-A_2005/061978 (2005年7月7日核發）揭示藉由 第一次分餾從LNG供料流移除氮氣，該第一次分餾提供富 含氮氣的塔頂物（「第一種蒸氣流」）及缺乏氮氣的底部液 體（「第一種液流」），並且對該底部液體進行第二次分餾 以提供比該第一種蒸氣流純度更低之富含氮氣的塔頂物 (「第二種蒸氣流」）及純化的LNG (「第二種液流」）。該 參 寺分餾可在塔或閃蒸罐中進行。該第二次分餾在比該第一 人刀餾更低的壓力下進行，並且該第一種液流可藉由膨脹 ^ 而冷卻，較佳地膨脹至或接近大氣壓力。該第一種蒸氣流 … 係，舉例來說呈燃氣渦輪燃料的形態，消耗掉，並且以不 超過相關設備可消耗的量產生。該第二種蒸氣流的唯一指 定用途為家用瓦斯。較佳地，該第一種蒸氣流具有1〇至 30莫耳％的氮氣含量而且該第二種蒸氣流具有低於5·5莫 耳％的氮氣含量。 發明内容 本务月的目的在於提供配合最小量的額外裝置及對於 設備效能最小的衝擊’從任何LNG製程剔除—部分氮氣。 這可藉由本發明，不需對用於LNG製造的熱傳導設備的結 構做任何改變，加上有限的額外設備就能達成。特別是， - I發明避免額外熱泵壓縮機的需求並且使咖最終產物能 '用於操作氮氣分離塔冷凝器。 在第一個也是最廣義的形態中，本發明提供一種從液 13 1273207 化天然氣供料移除氮氣之方法，該方法包含對該液化天然 氣進行第一次分餾以提供第一種富含氮氣的塔頂蒸氣流及 含氮氣的底部液流，並且對該底部液流至少一部分進行第 二次分餾以提供比該第一種塔頂蒸氣流純度更低的第二種 富含氮氣的塔頂蒸氣流及純化的液化天然氣流。 該第一種富含氮氣的塔頂蒸氣流可具有超過80莫耳％ 的氮氣濃度，較佳地超過90莫耳％，而且更佳地超過95 莫耳％。 通常，使該第一種富含氮氣的塔頂蒸氣流至少一部分 排至大氣並且以該第二種富含氮氣的塔頂蒸氣流作為，或 加至，燃料氣體，特別是用於燃氣渦輪，提供用於該天然 氣供料的液化相關用途的功。 較佳地，在利用該第一種富含氮氣的塔頂蒸氣的凝結 部分來迴流之蒸餾塔中進行第一次分餾。適當地，藉由包 含或衍生自至少一部分含氮氣的底部液流之低溫冷卻天然 氣流提供用於該凝結的熱交換功能。該低溫冷卻天然氣流 可為低溫冷卻及壓力降低之後全部或一部分含氮氣的底部 液流。該蒸餾塔可藉由該液化天然氣供料所提供的熱交換 功能使該蒸餾塔再沸。 同樣較佳為該第二次分餾在一閃蒸罐中進行。若該第 一次分餾在蒸餾塔中進行，該塔通常將利用位於該閃蒸罐 内之冷凝器所凝結的第一種富含氮氣的塔頂蒸氣之全部或 一部分來迴流。若凝結功能只需要一部分含氮氣的底部液 流，其餘部分可供至用於分成比該第一種塔頂蒸氣流純度 14 1273207 更低的第三種富含氮氣的塔頂蒸氣流及第二種純化的液化 天然氣流之第二個閃蒸罐。通常，該第三種富含氮氣的塔 頂蒸氣流將會與該第二種富含氮氣的塔頂蒸氣流結合在一 起，而且該第二種純化的液化天然氣流將會與來自第二次 分餾的純化的液化天然氣流結合在一起。 若該液化的天然氣供料流含有氦，可藉由，舉例來說， 局部凝結及分離以提供富含氦氣的蒸氣及富含氮氣的液 體，而從包含或衍生自該第一種富含氮氣的塔頂蒸氣之物 流分離富含氦氣的物流。用於該局部凝結的熱交換功能可 藉由所分離之富含氦氣的蒸氣及/或富含氮氣的液體提供。 在第二個形態中，本發明提供一種製備不含氮氣的液 化天然氣流之方法，包含液化含氮氣的天然氣以提供含氮 氣的液化天然氣流，並且根據先前第一個形態對該液化天 然氣流進行氮氣移除。 在本形態的較佳具體例中，製備不含氮氣的液化天然 氣流之方法包含： 將含氮氣的天然氣流供至具有液化與低溫冷卻段的螺 旋捲繞熱交換器中，其中藉由再循環的冷凍劑系統提供熱 交換器的冷凍功能，該冷凍劑系統係藉由燃料氣體供給動 力的燃氣滿輪供應功； 經過該液化段之後抽回液化氣流； 在蒸餾塔中對該液化氣流進行第一次分餾以提供第一 種富含氮氣的塔頂蒸氣流及含氮氣的底部液流； 使該底部液流至少一部分在該低溫冷卻段中低溫冷卻 15 1273207 並且使該部分降低壓力； 在一閃蒸罐中對該減壓部分進行第二次分餾以提供比 該第一種塔頂蒸氣流純度更低的第二種富含氮氣的塔頂蒸 氣流及純化的液化天然氣流； 在該閃蒸罐中凝結一部分第一種富含氮氣的塔頂蒸氣 流以提供在其中的熱功能並且產生凝結之富含氮氣的塔頂 物流； 使該凝結之富含氮氣的塔頂物流至少一部分以迴流的 方式返回該蒸餾塔；以及 使用該第二種富含氮氣的塔頂蒸氣流作為該燃料氣體 之至少一成分。 本發明另外提供一種藉由該第二個形態之方法用於製 備不含氮氣的液化天然氣流之裝置，該裝置包含： 用於液化該含氮氣的天然氣供料之冷凍系統； 一第一個分餾器； 一第二個分餾器； 用於將來自該冷凍系統之含氮氣的液化天然氣供至該 第一個分餾器的導管裝置； 用於從該第一個分餾器移除第一種富含氮氣的塔頂蒸 氣流的導管裝置； 用於將來自該第一個分餾器的含氮氣底部液體運送至 該第二個分餾器的導管裝置； 用於從該第二個分餾器移除該第二種富含氮氣的塔頂 蒸氣流的導管裝置；以及 16 1273207 裔移除該純化的液化天然氣流的 用於從該第二個分顧 導管裝置。
根據本發明的較佳且體 未完全地冷卻至其儲存條件 例，令已經在壓力下液化但尚 的天然氣降至中等壓力，並且 供入第一個氮氣分離塔中。 生具有降低氮氣含量的底部 終燃料氣體的氮氣含量之目 該LNG物流閃蒸至此塔内將產 液體。此降低的量就是降低最 的所想要的。使從此塔底部抽 取的LNG進一步冷名p $导攸/ 取〜閃療系統所需的溫度以製造具 有最終預期氮氣含量的LNG θ θ 士 & & & ^ NCj及具有所需熱值的燃料氣體。 將此最後冷卻的LNG傳送至最終閃蒸罐。該最終閃蒸罐含 有熱交換ϋ ’該熱交換器係用於凝結該氮氣分離塔的塔頂 蒸氣流並且提供迴流給此塔。此塔的塔頂蒸氣係可直接地 排至大氣中的氮氣流。
供至該塔的塔頂蒸氣冷凝器可整合至該方法的最終閃 蒸罐内，在該例中所有的產物LNG都通過此罐。可視需要 地只許一部分LNG產物可通過此罐。 该氮氣分離塔可具有再沸器，該再沸器係於壓力降低 之别藉由供至該塔的LNG供料再沸，視需要地經過流體膨 脹器。 來自該塔頂部的氮氣產物可被膨脹並且從彼將冷束劑 回收至在該LNG方法中被冷卻或液化的物流中。 本發明特別有用於使用供LNG液化用之螺旋捲繞熱 交換裝置的LNG設備。只要在該液化段之後抽取該含有氮 氣的LNG並使其在較低壓力下返回，並且在該低溫冷卻段 17 1273207 中耗掉氮氣並取得用於冷凍的1^^(}最終產物。關於C3Mr 方法，這可簡單地在倒數第二段與最末冷凍階段之間抽取 並送返LNG，並且使用半成品LNG而達成。同樣地關於 AP X ，可在主要的低溫熱交換器與該低溫冷卻器之間抽 取並送返LNG，並且使用半成品LNG。 幾乎該供料氣體所含的任何份量之氮氣都可藉由本發 明以純氮氣流的形態被剔除。 實施方式 本發明的例示具體例可應用於任何化方法，其 中有液化^又，接著一低溫冷卻段。舉例來說，可配合氮 氣膨脹器循％ LNG低溫冷卻（Αρ-χ)方法以及舉例說明的 C3MR方法應用於兩種或雙重混合的冷凍劑（dm…及混成 C3MR預~卻及液化。該LNG係於液化與低溫冷卻段之間 引用’供至氮氣分離塔，氮氣在那裏以「純的」形式剔除。 使孩LNG返回該低溫冷卻段，之後使用該產物的部 刀β度來操作該氮氣分離塔冷凝器。 對妝第1圖，在預處理單元2中預處理天然氣流供料 1以移除例如水及二氧化碳等的雜質，該等雜質在該設備 的低溫段中不那樣冷;東。使所得不含雜質的供料氣體3在 “或夕個熱交換器4中預先冷卻，在那之後使其通入分離 塔7。該（等）熱交換器可為一系統的熱交換器（4、5_參見第 2及3圖）’混合冷康劑係於其中蒸發。塔7使蒸發的物流 刀成車工貝i合頂条氣部分i 〇及重質底部液體部分9，其含 18 1273207 有該LNG產物不想要的重質成分。靠冷凝器u中的冷凍 劑局部地凝結該塔頂蒸氣1 〇。在分離器40中分離該局部 凝結的物流13以提供液態凝結物14，其經由泵丨2以迴流 的方式重返該分離塔7，以及塔頂蒸氣丨5，其係供至捲繞 的熱交換器16。使該塔頂蒸氣進一步在該熱交換器16的 第一段中冷卻至該冷卻物流17維持實質上液態的溫度，同 時藉由膨脹閥或膨脹渦輪1 8降至中等壓力。憑藉呈物流 • 2 7的形式排出熱父換器16的混合冷凍劑物流在該熱交換 器1 6中進行冷卻。 . 在一或多個壓縮器28、30中壓縮該混合冷凍劑。該壓 縮的混合冷凍劑先靠冷卻器3 1中的冷卻介質冷卻，然後靠 冷卻器3 2至3 5中的弟一種預冷卻的冷柬劑進一步冷卻並 且局部地凝結。在分離器3 7中分離局部凝結的冷凍劑，並 且將蒸氣及液體部分二者供至該液化熱交換器1 6。 等壓力降低之後’在氮氣剔除塔23中分離該物流4 1 φ 以提供底部液體19及塔頂蒸氣46。與供至該塔23的供料 41相比该底部液體19具有降低的氮氣含量，並且靠混合 冷凍劑在該熱交換器16的第二部分中進一步冷卻至其維 持實質上維持液態的溫度，同時降至該LNG產物所想要的 壓力。使該冷的LNG物流20橫跨膨脹閥21而降低歷力， 並且使該低壓物流42通入閃蒸罐25，該低壓物流42在其 •中局部地蒸發以提供液態產物LNG部分5〇及蒸氣燃料部 分36。藉由熱交換器24提供在該閃蒸罐25中的熱交換功 忐，使來自該氮氣剔除塔23的塔頂蒸氣流46之一部分在 19 1273207 頂蒸氣流46的其餘部分26，其 該熱交換器24凝結。該& 具有較高純度的氮氣，排 /土十^ + 辨至大虱。使來自該熱交換器24 凝結氮氣44以迴流45的方彳％ 兮#〆 曰]万式返回该虱氣剔除塔23。液能 氮氣物流22可視需要铋ρ抓na ,丨 /心 而罟地攸離開凝結器24的凝結物流料抽 第2圖的具體例與第」圖的不同之處在於將再濟哭ο 力:至該氮氣剔除塔23，增加膨脹器49使該供料膨服:該 塔23，亚且增加熱交換器57以便從該塔23的塔頂蒗氣呻 分2、2及/或該閃蒸罐25的塔頂蒸氣部分回收冷康劑。^ 而，这些特徵各自都可單獨地使用或與該氮氣剔除塔幻相 關聯而以任何組合的方式使用。 該再沸器47位在塔23的底部以提高該塔所剔除的氮 亂里。使用來自該熱交換器i 6第一段的冷卻高壓供料氣體 17以提供再沸器47的熱功能，並且使離開該再沸器47的 所得物流48在通入塔23之前先在膨脹渦輪49中膨脹。 冷凍劑可從來自塔23及閃蒸罐25的塔頂蒸氣26及 36其中之一或二者回收。這可藉著使相關的物流通至熱交 換57而進行，而且若有必要使來自該氮氣剔除塔的暖化 塔頂蒸氣58在渦輪膨脹器59中膨脹。藉由該熱交換器57 所回收的冷凍劑予以冷卻的物流61可為供料氣體或循環 冷凍劑的側流。 第3圖的具體例與第1圖的具體例不同之處在於並非 所有的冷LNG物流20都通過該閃蒸罐25。而是，該冷的 LNG物流2〇分成第一物流53，令其向下供入第二個閃蒸 20 1273207 罐52，並且令第二物流54向下供入閃蒸罐25。收集離開 閃蒸罐25及52的蒸氣並且結合成物流56，將其傳送至該 燃料氣體系統。結合離開閃蒸罐25及52的LNG液流5〇 及5 1並且以物流的形式傳送至LNG儲存槽。
第4圖的具體例與第1圖的具體例不同之處在於該熱 乂換16的第二部分由單獨的熱交換器6〇來代替。熱交 換器1 6及60各自使用不同的冷凍劑流體。來自該氮氣剔 除塔23的底部液體19通至該熱交換器6〇，其中靠適合的 第三種冷凍劑62、63冷卻該底部液體19，該冷凍劑62、 63可為混合冷凍劑或例如氮氣等的純流體。來自該熱交換 态60的冷LNG物流2〇提供該供料至該閃蒸罐25。 本發明另一個具體例係有關從該氮氣剔除塔23的塔 頂蒸氣46回收富含粗製氦氣流。在舉例來說，第丨圖的具 體例中该塔頂蒸氣46的排放部分26經常都在磅/平方 如^胃萬⑹左右的壓力及指外⑹以的溫度下] 忒：料氣體含有氦氣’在該供料氣體中的氦氣有一大部分 係含於此物流26並且可利用第5圖的處理機制從物流％ 輕易地得到。靠熱交換器7G中的返回氮氣流％及氛氣流 來7郃物机26。物流71離開熱交換器7〇局部地凝結並 在刀：罐72中分成液體部分75及蒸氣部分73。物流 73 ’其實質上為氦齑 仫 > 札係於熱父換為70甲再暖化並且輸出 所^的粗製氦氣流78以供進一步純化。物流75，其實質 ’係横跨閥門74而降嶋，並且使所得的冷卻 -在該熱交換器70中再暖化，並且所得的物流”可 21 1273207 再暖化以便在排至大氣之前先回收另外的冷凍劑。 貫施例1 本貫施例係基於第1圖的具體例。該LNG方法以 88,0〇〇磅莫耳/小時（4〇,〇〇〇公斤莫耳/小時）供應在室溫及 900磅/平方吋（6.2百萬帕）壓力下之含4·8莫耳％氮氣的天 然氣供料，其餘部分主要為甲烷。乾燥並且預冷卻該供料 • 氣體’並在分離塔7中預熱使其於_38〇F (-39c>c)的溫度及 約850碎/平方吋（5·8百萬帕）的壓力下進入熱交換器16。 • 物流17在-178叩（-116.5。0)的溫度下離開熱交換器16，並 且在供至該氮氣剔除塔23之前先使壓力降至22〇磅/平方 对（1.5百萬帕），該氮氣剔除塔23在220磅/平方吋（1·5百 萬帕）下操作。從該塔23的底部抽取物流19並且在熱交換 器16中進一步冷卻至_247〇F (_155〇c)。然後使離開該熱交 換器16的物流20降至低壓進入閃蒸罐25中。從溫度-261 φ G163。0)的閃蒸罐25抽取LNG產物流50，氮氣含量低於 1·5莫耳％。以7,900磅莫耳/小時（3,600公斤莫耳/小時）的 流速從閃蒸罐25抽取燃料物流36，氮氣含量低於3〇莫耳 %。以600磅莫耳/小時（272公斤莫耳/小時）的流速從塔23 的頂部抽取氮氣排出物流26，氮氣含量低於98.0莫耳％並 且溫度-257°F (-160.5。〇。 實施例2 本實施例係基於第丨圖的具體例，含第5圖粗製氦氣 22 i2732〇7 抽取的增加。該LNG方法以88,〇〇〇磅莫耳/小時（4〇,〇〇〇公 斤莫耳/小時）供應在室溫及900磅/平方吋（6·2百萬帕）壓力 下之含4.8莫耳％氮氣及6〇〇 ppmv氦氣的天然氣供料，其 餘部刀主要為甲烷。乾燥並且預冷卻該供料氣體，並在分 離塔7中預熱使其於·38α；ρ (-39〇c)的溫度及約8“./平方 吋（5·8百萬帕）的壓力下進入熱交換器16。物流17在_178吓 (-116.5°C)的溫度下離開熱交換器16，並且在供至該氮氣剔 除塔23之前先使壓力降至22〇磅/平方吋（15百萬帕），該 氮氣剔除塔23在220磅/平方吋（1·5百萬帕）下操作。從該 • 塔23的底部抽取物流19並且在熱交換器16中進一步冷卻 • 至-247^ (-155〇C)。然後使離開該熱交換器16的物流2() 降至低壓進入閃蒸罐25中。從溫度_261〇F (-163°C)的閃蒸 罐25抽取LNG產物流50，氮氣含量低於15莫耳％。以 7,900 %莫耳/小b寸（3,600公斤莫耳/小時）的流速從閃蒸罐 25抽取燃料物流36,氮氣含量低於3〇莫耳％。以71〇磅 魯莫耳/小時（322公斤莫耳/小時）的流速從塔23的頂部抽取 氮氣排出物流26，氮氣含量低於98 〇莫耳％並且溫 度_259吓（-161.5。〇,並且壓力22〇磅/平方吋（1·5百萬 帕）。對照第5圖，靠返回物流73及76使物流％在熱交 換器70中冷卻至-298〇F (-i83.5〇c)的溫度，並且在分離器 72中分成液流及瘵氣流。使該液流降至低壓以提供焦耳湯 姆生冷凍作用而物流76達到_31〇。1? (_19〇〇c)的溫度。在交 • 換器70中再暖化液流76及蒸氣流72。物流77為具有656 磅莫耳/小時（297.5公斤莫耳/小時）流動及97 5%氮氣含量 23 很顯然本發明並不限於以上所揭 例的詳細内容，並且可進行許多修飾 後續申請專利範圍所定義的發明範圍
1273207 的氣氣排出物流。物流78為具有54磅莫耳/小時(24 5公 斤莫耳/小時）流動及74%氦氣濃度的氦氣產物流。 示有關該等例示具體 及變化而不會悖離如 圖式簡單說明 底下僅藉由實施例的方式並且泉昭 、， ^ 本發明目丽較佳的 具體例的附圖來說。在該等圖式中： 第1圖顯示應用於丙烧預冷卻混合冷康劑（C3MR^ LNG設備之基本原理’該設備使用單—捲繞的熱交換器來 液化並且低溫冷卻； 第2圖顯示第！圖的具體例的修飾例，其併入用於該 氮氣剔除土合的再沸器、用於供至贫拔沾 K 主这J合的供料之膨脹器，及 從該塔頂蒸氣回收冷凍劑的熱交換器； 第3圖顯示第i圖的具體例的修飾例，其中只用一部 分LNG物流提供凝結功能； 第4圖顯示第1圖的具體例的修飾例，其中由單獨的
熱交換11 60代替該捲繞的熱交換器的第二部分；以及 第5圖顯示用於從該LNG 认乳虱 < 弟1圖的具體例 的修飾例。 24 1273207
元件符號說明 1 天然氣流供料 2 3 不含雜質的供料氣體 4 5 熱交換器 6 7 分離塔 9 10 塔頂蒸氣 11 12 泵 13 14 液態凝結物 15 16 熱交換器 17 18 膨脹渦輪 19 20 LNG物流 21 22 液態氮氣物流 23 24 熱交換器 25 26 塔頂蒸氣流的其餘部分 27 28 壓縮器 30 31 冷卻器 32 33 冷卻器 34 35 冷卻器 36 37 分離器 40 41 物流 42 44 凝結氮氣 45 46 塔頂蒸氣流 47 48 物流 49 50 液態產物LNG部分 51 52 第二個閃蒸罐 53 54 第二物流 56 57 熱交換器 58 59 渦輪膨脹器 60 61 物流 62 63 冷凍劑 65 70 熱交換器 71 72 分離罐 73 74 閥門 75 76 返回氮氣流 77 78 粗製氦氣流 預處理單元 熱交換器 蒸發的物流 底部液體 冷凝器 局部凝結的物流 塔頂蒸氣 冷卻物流 底部液體 膨脹閥 氮氣剔除塔 閃蒸罐 物流 壓縮器 冷卻器 冷卻器 蒸氣燃料部分 分離器 低壓物流 迴流 再沸器 膨脹渦輪 LNG液流 第一物流 物流 暖化塔頂蒸氣 熱交換器 冷凍劑 物流 物流 乱氣流 液體部分 物流 25

Claims (1)

1273207 十、申請專利範圍： 1· 一種從液化天然氣供料（41)移除氮氣之方法，包含在蒸 餾塔（23)中對該液化天然氣進行第一次分餾以提供第一 種富含氮氣的塔頂蒸氣流（46)及含氮氣的底部液流 (19);使該底部液流（19)至少一部分低溫冷卻（16)且降低 壓力（21)，並且對該部分進行第二次分餾以提供比該 第一種塔頂蒸氣流（46)純度更低的第二種富含氮氣的塔 頂瘵軋/现（36)及純化的液化天然氣流，其中該蒸鶴塔利 用一部分凝結以供該第二次分餾（25)的熱交換功能之第 種萄含氮氣的塔頂蒸氣流（46)來迴流，其特徵為該第 二次分餾在一閃蒸罐（25)中進行。 2·如申請專利範圍第1項之方法，其中藉由非衍生自該液 化天然氣供料的冷凍劑（39)提供該低溫冷卻〇幻的冷凍 功能。 3 ·如申請專利範圍第1或2項之方法，其中以該第二種富 含氮氣的塔頂蒸氣流6)作為，或加至，燃氣渦輪的燃 料氣體，提供用於液化該天然氣供料（41)相關的功。 4·如申请專利範圍第丨或2項之方法，其中全部含氮氣的 底部液流（19)係供至該閃蒸罐（25)。 5·如申請專利範圍第1或2項之方法，其中只有一部分（54) 该低溫冷卻之含氮氣的底部液流（2〇)係供至該閃蒸罐 (25) ’而且其餘部分（53)係供至用於分成比該第一種塔頂 条氣流（46)純度更低的第三種富含氮氣的塔頂蒸氣流（55) 及第一種純化的液化天然氣流（5 1)之第二個閃蒸罐（52)。 26 1273207 6_如申請專利範圍第i或2 貝之方法，其中該第一種富含 氮氣的塔頂蒸氣流（46)具有超 7 ^ ^ ,韦超過8〇莫耳〇/〇的氮氣濃度。 Π請t利範圍第…項之方法，其中該第一種富含 鼠孔的塔了頁条氣流（46)具有超過9〇莫耳〇/〇的氮氣濃度。 :請專利範圍第…項之方法，其中該第一種富含 I礼的塔頂瘵氣流(46)具有超過％莫耳％的氮氣濃度。
9· 一種製備不含氮氣的液化天然氣流（5〇)之方法，包含液 化各氮氣的天然氣（15)以提供含氮氣的液化天然氣流7, 4 U ’並且在蒸餾塔（23)中對該液化天然氣進行第一次分 餾以提供第一種富含氮氣的塔頂蒸氣流（46)及含氮氣的 底σ卩液心（1 9),使该底部液流（丨9)至少一部分低溫冷卻 (16)且降低壓力（2丨），並且對該部分進行第二次分餾（25) 以提供比該第一種塔頂蒸氣流（46)純度更低的第二種富 含氮氣的塔頂蒸氣流（36)及純化的液化天然氣流，其中 该蒸餘塔利用一部分凝結以供該第二次分餾（25)的熱交 換功能之第一種富含氮氣的塔頂蒸氣流（46)來迴流，其 特徵為該第二次分餾在一閃蒸罐（25)中進行。 10·如申請專利範圍第9項之方法，其中該含氮氣的天然氣 (1 5)係於具有液化與低溫冷卻段的螺旋捲繞熱交換器（16) 中液化，經過該液化段之後抽回該含氮氣的液化天然氣 流並且在該低溫冷卻段中低溫冷卻來自該蒸餾塔（23)的 底部液流。 U·如申請專利範圍第9或10項之方法，其中以該第二種 富含氮氣的塔頂蒸氣流（36)作為，或加至，用於燃氣渦 27 1273207 輪的燃料氣體，提供用於該天然氣供料（4 1)液化相關用 途的功。 12·如申請專利範圍第10項之方法，包含·· 將含氮氣的天然氣流（15)供至具有液化與低溫冷卻段的 螺旋捲繞熱交換器（16)中，其中藉由再循環的冷凍劑系統 (27-89)提供熱交換器的冷凍功能，該冷凍劑系統（27_89)係 藉由燃料氣體供給動力的燃氣渦輪供應功；
經過該液化段之後抽回液化氣流（1 7); 在条館i合（23)中對该液化氣流進行第一次分顧以提供第 一種富含氮氣的塔頂蒸氣流（46)及含氮氣的底部液流（19); 使該底部液流（19)至少一部分在該熱交換器（16)的低溫 冷卻段中低溫冷卻並且使該部分降低壓力（2丨）· 在一閃蒸罐（25)中對該減壓部分進行第二次分餾（25)以 提供比該第一種塔頂蒸氣流（4 6)純度更低的第二種富含氮 氣的塔頂蒸氣流（3 6)及純化的液化天然氣流（5〇) · 在該閃蒸罐中凝結-部分第-種富含氮氣的塔頂基氣流 以提供在其中的熱功能並且產生凝結之富含氮氣的 流（44); 、 、 使邊滅結之畐含氮氣的塔頂物流至. 士~部分（45)以迴流 的方式返回該蒸餾塔（23);以及 使用該第二種富含氮氣的塔頂蒸氣 體之至少-成分。、 ❿)作為該燃料氣 13·—種藉由如申請專利範圍第9項之 〈万法用於製備不合新 氣的液化天然氣流之裝置，該裝置包含· 火 28 1273207 用於液化該含氮氣的天然氣供料（丨 -一蒸餾塔（23); 冷凍系統（16); 一閃蒸罐（25); 在該閃蒸罐（25)内之冷凝器（24); 之熱交換器（I6); 氣的液化天然氣供至 用於接受冷凍流體（39)的冷凍功能 用於將來自該冷凍系統（丨6)之含氮 該蒸餾塔（23)的導管裝置（17, 4υ ;
用於攸该蒸顧塔（23)移除第一種富含 的導管裝置（46); 氮氣的塔頂蒸氣流 用於將該第一種富含氮氣的塔頂墓教 …、虱成之一部分運送至 該冷凝器（25)的導管裝置（43); »用於使來自該冷凝n(25)之凝結㈣第_種富含氣氣的 塔頂蒸氣流以迴流的方式返回至該蒸館塔（2 3)的導管震置 (44, 45);
用於將來自该瘵餾塔（23)之含氮氣的底部液流運送至該 熱交換器（24)的導管裝置（19); 用於將來自该熱父換益之低溫冷卻的含氮氣底部液流運 送至減壓下的閃蒸罐（25)的導管裝置（2(^ ; 用於從該閃蒸罐（25)移除該第二種富含氮氣的塔頂蒸氣 流的導管裝置（36);以及 用於從該閃蒸罐移除該純化的液化天然氣流的導管裝置 (50) 〇 14.如申請專利範圍第π項之裝置，進一步包含提供用於 該天然氣供料（41)液化相關用途的功之燃氣渦輪，及用 29 1273207 於將為第一種畐含氣氣的塔頂蒸氣流以燃料氣體供料的 方式供至該燃氣渦輪的導管裝置（3 6)。 1 5 ·如申請專利範圍第13或14項之裝置，其中該冷來系統 包含具液化與低溫冷卻段的螺旋捲繞熱交換器（丨6);經 過該液化段之後用於將含氮氣的液化天然氣供至該蒸鶴 塔（23)的導管裝置（I7，41)從該熱交換器抽回該氣流；並 且由該低溫冷卻段構成使來自该該蒸餾塔（2 3)之含氮氣 的底部液流低溫冷卻的熱父換為（1 6)。
30
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NO20075947L (no) 2007-11-19
EP1872072A1 (en) 2008-01-02
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AU2006238748B2 (en) 2010-04-01
US20070245771A1 (en) 2007-10-25
EP1715267A1 (en) 2006-10-25
CA2605545C (en) 2010-11-02
CN101163934A (zh) 2008-04-16
US7520143B2 (en) 2009-04-21
WO2006111721A1 (en) 2006-10-26
RU2355960C1 (ru) 2009-05-20
KR20080010417A (ko) 2008-01-30
CN101163934B (zh) 2012-03-14
KR100939515B1 (ko) 2010-02-03
TW200638013A (en) 2006-11-01
JP4673406B2 (ja) 2011-04-20
JP2008537089A (ja) 2008-09-11
NO343069B1 (no) 2018-10-22
CA2605545A1 (en) 2006-10-26
EP1872072B1 (en) 2018-08-01
MX2007013033A (es) 2008-01-11
AU2006238748A1 (en) 2006-10-26

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