TWI313186B - Removing natural gas liquids from a gaseous natural gas stream - Google Patents

Removing natural gas liquids from a gaseous natural gas stream Download PDF

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TWI313186B
TWI313186B TW093102744A TW93102744A TWI313186B TW I313186 B TWI313186 B TW I313186B TW 093102744 A TW093102744 A TW 093102744A TW 93102744 A TW93102744 A TW 93102744A TW I313186 B TWI313186 B TW I313186B
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stream
natural gas
gaseous
liquid
overhead
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TW093102744A
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TW200505548A (en
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Eduard Coenraad Bras
Paramasivam Senthil Kumar
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Shell Int Research
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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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • 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
    • 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
    • F25J3/0204—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 feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • 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
    • 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
    • F25J3/0204—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 feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • 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
    • 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
    • F25J3/0233—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
    • 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
    • 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
    • F25J3/0238—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 2 carbon atoms or more
    • 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
    • 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
    • F25J3/0242—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 3 carbon atoms or more
    • 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
    • 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Chemical & Material Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Gas Separation By Absorption (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Description

1313186 玖、發明說明： 【發明所屬之技術領域】 本發明係關於從氣態天然氣物流中移除天然氣液態物 質。在說明書與申請專利範圍中，術語天然氣液態物質是 用以指稱較重的碳氫化合物’像是液化石油氣成份與天然 汽油。 【先前技術】 因為天然氣液態物質具有經濟價值且因為移除天然氣 液態物質會降低天然氣物流的熱值，所以將天然氣液態物 質移除。 透過實例我們給定天然氣液態物質要被移除的天然氣 物流之莫耳組成為：甲烷86莫耳％，乙烷6莫耳％，丙烷 4莫耳％，丁烷略高於i莫耳％，而其餘量則由其他成份像 是氮氣、二氧化碳和氦氣形成。 本發明尤其關於在提高的壓力，例如在大於3 Μρ& ( 絕對壓力）和小於天然氣的臨界壓力，其為約7 Mpa (絕 對壓力）t壓力下從天然氣物流中移除此天然氣液態物質 USA專利說明書第5 325 673號揭露一種從天然氣物 流移除較重碳氫化合物的方法，此公開揭露一種為了液化 作用而預先處理較重碳氫化合物之方法，其是藉由從中移 除較重碳氳化合物，包括以下步驟： a)將天然氣進料物流導人具有上增濃段與下汽提區段 的洗務塔中； 1313186 b)將進料物流與導入塔之上增濃區段的液態回流物流 接觸，以吸收進料物流中的C5+碳氫化合物； + C)回收含有C2-C4碳氫化合物與具有小於約i ppm之 C6碳氫化合物濃度的塔頂蒸汽產物； d) 再沸塔下區段内的部分液體，以從進料物流中移除 較輕的碳氫化合物； e) 回收§含C/碳氫化合物的液態塔底產物；以及 f) 操作塔以獲得主要存在於塔頂產物中的C2_C4碳氫 化合物。 此習知方法是針對於獲得具有很低碳氫化合物濃 度的塔頂產物，然而，塔頂產物仍然含有相當多量的乙烷 、丙烷與丁烷。 【發明内容】 本發明提供一種從氣態天然氣物流中移除天然氣液態 物質的方法，其中獲得高壓分離，其具有高的丙烷回收率 以及高的曱烷與乙烷移除量。此外，本發明之目的在於提 供一種移除天然氣液態物質的方法，其中不需任何再沸器。 為達此目的，本發明於提高壓力下從氣態天然氣物流 中移除天然氣液態物質，以獲得具有減少含量之天然氣液 悲物質之氣態產物流的方法，包括以下步驟： (a) 將天然氣物流冷卻； (b) 將冷卻的天然氣物流導入具有下汽提區段及上吸收 區#又的洗滌塔之底部，每一區段含有至少一個理論階； (c) 使天然氣通過洗滌塔上升，並從洗滌塔頂部移除拔 1313186 除塔頂物流； (d) 部分冷凝此塔頂物流，及將此部分冷凝的塔頂物流 分離成具有減少含量之天然氣液態物質的氣態物流以及液 態回流物流’並將氣態物流以具有減少含量之天然氣液態 物質的氣態產物流移除； (e) 將液態回流物流分成第—回流物流與第二回流物流 (f) 將第一回流物流導入洗滌塔的吸收區段頂部； (g) 將第二回流物流導入汽提區段的頂部，以去除所要 的輕質氣態成份；以及 ⑻從洗料柱底部移除富含較重成份的液態底部物流 〇 適當地，依據本發明之方法更包含將碳氫化合物液體 導入吸收區段的頂部。 【實施方式】 現將藉由實例以及參考隨附圖式來詳細說明本發明， 其中 圖1為本發明第一具體實例之流程圖；以及 圖2為本發明第二具體實例之流程圖。 百先請參照圖1。將包含天然氣液態物質（C2-C4碳氫 化合物與C5 +碳氯化合物）之氣態天然氣物流（其本質上不 3酉文氣）―工由導官1供應至熱交換器2，該物流於熱交換 态2中被部分冷凝。部分冷凝的天然氣經由導管3供應至 洗知'塔6的底部。進入洗滌塔的天然氣壓力介於3至7 MPaG’e對壓力）之間’且溫度介於g至-別。^。 1313186 洗務塔6於供應天然氣之壓力下操作。洗務塔6包含 兩個區域’下汽提區7以及藉由間隔9而與汽提區7隔開 的上吸收區段8。汽提區段7包含介於ι 1 4個理論階， 而吸收區段8包含介於4至1〇個理論階。理論階可藉由 接觸盤或適當的填裝材料來提供。 天然氣物流的氣態餾份係容許在洗滌塔6上升通過汽 提區段7與吸收區段8。天然氣物流之液態德份係經由導 管1 〇從洗滌塔6移除。 從洗滌塔6的頂部，經由導管12移除塔頂物流，該 塔頂物流具有減少含量的天然氣液態物質。該塔頂物流於 熱父換器14中部分冷凝，並於分離容器17中分離成液態 物流與氣態產物流。氣態產物流經由導管2〇移出分離容 器17，並流向使氣態產物流液化的工廠（未顯示）。從導 管21移除液態物流。部分冷凝之塔頂物流的溫度是介於_ 25至-65°C的範圍間，且在部分冷凝之塔頂物流内的液體 含量是介於10至35莫耳％ (以總塔頂物流為基準）之間 。適當地，在將氣態產物輸送離開之前，可將從導管2〇 移除的氣態產物流供應至熱交換器14 (未顯示），以提供 用於部分冷凝塔頂物流之冷卻。 經由導管22將部分的液態物流當作第一回流物流導 入洗務塔6之頂部的吸收區段8上方中作為吸收劑。將此 液體帶到吸收區段8中而與來自汽提區段7的氣體產生逆 流接觸。比曱烧要重之成分則藉由作為吸收劑的第一回流 物流而從氣體中移除。 1313186 將液態物流之剩餘物當作第二回流物流以經由導管23 導入洗;條塔6内位於汽提區段7上之間隔9中。在汽提區 ^又7中’將第二回流物流和從吸收區段8下降的液體與天 然规1物流的上升氣態餾份產生逆流接觸。氣態餾份從液態 物流中脫除輕質成份（曱烷和乙烷）。之後將具有低濃度 之輕質成份的液態物流經由導管10從洗滌塔6的底部移 除。 適當地’在導管23中第二回流物流之含量是佔從分 離谷器1 7移除之液態物流的1 〇至95重量。/()之間。 另外’可將碳氫化合物液體經由導管25導入吸收區 段8的頂部。適當的碳氫化合物液體為丁烷。適當地，此 額外吸收劑的含量經由導管22供應之液體量的1至4倍 。適當地’此額外的吸收劑是由丁烷附加物成份所組成。 現請參照圖2。請注意，在圖1所討論之元件將給予 相同的符號，而將不在此討論。將經由導管1 〇移除的液 態塔底物流導入汽提塔30的頂部，以從液態塔底物流中 脫除氣態成份，像是甲烷和乙烷。汽提塔30具有包括至 少一個理論分離階的汽提區段3 3。汽提區段3 3適當地包 括2-10個理論分離階。在汽提塔30内的壓力為介於2_3.5 MPa (絕對塵力）的範圍。為了使液態塔底物流的廢力得 以減低，導管10包括壓力減低閥34。 液態物流係從汽提塔30底部經由導管35移除。部分 液態塔底物流於再沸器36内汽化，並將所得蒸汽導入汽 提塔30的底部。剩餘物則經由導管38流出離開至赌槽（ 11 1313186 未顯示）或至另一個處理（未顯示）。 汽態塔頂物流則從汽提塔30頂部經由導管4〇移除。 氣態塔頂物流則於熱交換器43内部分冷凝以獲得部分冷 凝的氣態塔頂物流。於分離器46中將部分冷凝的塔頂物 流分離成液態餾份與氣態餾份。將液態餾份從導管48移 出並當作回流導入汽提塔30的頂部。將氣態餾份經由導 管5 0移出並加入氣態產物流中。視情況需要地，使用壓 縮機53將氣態塔頂餾份的壓力增加至氣態產物流的壓力 〇 適當地，將經由導管20移出的至少一部份之氣態產 物流供應至熱交換器14 ’以提供用於部分冷凝塔頂物流 12之冷卻。 適當地，氣態塔頂德份係藉由與經由導管20供應至 熱交換器43的氣態產物流間接熱交換而部分冷凝。 適當地，經由導管1 〇而從洗滌塔6移除之液態塔底 物流係藉由在熱交換器55内與氣態產物流間接熱交換而 冷卻。 於熱交換器2中，將導管1内的天然氣物流部分冷凝 ’且此係適當地藉由與氣態產物流間接熱交換而進行。 適當地，供應至洗滌塔6之碳氫化合物液體係在熱交 換器5 7中藉由與氣態塔頭顧份間接熱交換以冷卻。 現藉由實例方式，以參考三組計算實例來說明本發明 。於第一個實例中，並非依據本發明，僅將經由導管22 的回流供應至洗滌塔6的頂部。於第二個實例中，依據本 12 1313186 發明’經由導管 依據本發明，铖·、 3供應回流。而於第三個實例中， 每-個實例中2 ^ 25供應額外的碳氫化合物液體。 回收最大化 ”作條件係經選擇以使天然氣液態物質的 ;斤有貫例中，洗滌塔含有八個理論分離階。於兩個 依據本發明的實例φ，、士坦厂饥 、彳中/飞提& ^又7含有二個理論分離階， 而吸收區段8含有六個理論分離階。 其結果係摘述於下表1 · 8中。 於表中’莫耳流速的單位為krn〇i/s，質量流速的單位 為kg/s，溫度的單位為。c，壓力的單位為Mpa (絕對壓力 )’而莫耳組成的單位為mol%。丁烷附加物成分為丁烷 異丁烷、戊烷、異戊烷、己烷以及庚烷。在組成中提及 的其它成份為水、氮氣、硫化氫、二氧化碳以及氦氣。 13 1313186 表1.經由導管3供應部分冷凝進料的數據 物流3 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 7.90 7.55 7.73 質量流速 155 142 145 溫度 0 -5 -5 壓力 5.6 5.8 6.0 莫耳組成 甲烷 0.862 0.882 0.882 乙烷 0.064 0.062 0.062 丙炫 0.042 0.036 0.036 丁烷附加物 0.031 0.019 0.019 其他成份 餘量 餘量 餘量 14 1313186 表2.從洗滌塔頂部經由導管12移除的塔頂物流之數據。請注意因 為内部回收，其流速大於導管3内的流速。 物流12 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 8.79 8.64 8.39 質量流速 168 161 152 溫度 -19 -23 -18 壓力 5.6 5.6 6.0 莫耳組成 甲烷 0.852 0.871 0.897 乙烷 0.080 0.078 0.070 丙烧 0.064 0.043 0.022 丁烷附加物 0.003 0.006 0.001 其他成份 餘量 餘量 餘量 15 1313186 表3.經由導管22供應至洗滌塔6頂部的回流的數據 物流22 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 1.57 0.17 0.08 質量流速 40.5 4.05 1.81 溫度 -43 -48 -54 壓力 5.6 5.8 6.0 莫耳組成 曱烷 0.571 0.650 0.720 乙烷 0.176 0.170 0.155 丙烧 0.241 0.152 0.078 丁烷附加物 0.001 0.027 0.005 其他成份 餘量 餘量 餘量 16 1313186 表4·經由導管23供應至洗滌塔6中汽提區段7頂部的回流的數據 物流23 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 不適用 1.54 1.46 質量流速 不適用 3.68 3.31 溫度 不適用 -48 -54 壓力 不適用 5.8 6.0 莫耳組成 甲烷 不適用 0.650 0.720 乙烷 不適用 0.170 0.155 丙烧 不適用 0.152 0.078 丁烷附加物 不適用 0.027 0.005 其他成份 不適用 餘量 餘量 17 1313186 表5.經由導管25供應至洗滌塔6頂部的碳氫化合物液體的數據 物流25 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 不適用 不適用 0.12 質量流速 不適用 不適用 7.9 溫度 不適用 不適用 -33 壓力 不適用 不適用 6.0 莫耳組成 甲烷 不適用 不適用 0.00 乙烧 不適用 不適用 0.00 丙烧 不適用 不適用 0.00 丁烷附加物 不適用 不適用 1.00 其他成份 不適用 不適用 0.00 18 1313186 表6.從導管20移除的氣態產物流的數據 物流20 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 7.196 6.927 6.852 質量流速 128 120 109 溫度 -43 -49 -54 壓力 5.3 5.5 5.7 莫耳組成 曱烷 0.913 0.925 0.937 乙烷 0.059 0.055 0.051 丙炫 0.026 0.017 0.009 丁烷附加物 0.0009 0.0011 0.0015 其他成份 平衡 平衡 平衡 19 1313186 表7.從洗滌塔6底部經由導管10移除的進料氣體之液體餾份的數據 物流10 實例1， 非依據本發明 實例2， 依據本發明 實例3， 依據本發明 莫耳流速 0.70 0.63 0.99 質量流速 27 22 36 溫度 -2 -11 -10 壓力 5.6 5.8 6.0 莫耳組成 曱烷 0.343 0.401 0.401 乙烷 0.108 0.133 0.133 丙烧 0.208 0.255 0.218 丁烷附加物 0.341 0.210 0.247 其他成份 餘量 餘量 餘量 藉由比較從洗滌塔6底部經由導管10移除的液態物 流中的碳氳化合物含量，可將結果摘述於表8中。 20 1313186 組成，其按經由 到最後一個實例 I 8.經"由導管1 〇移除的液態物流之 導管1供應的進料組成之百分比計（考慮 中、、、二由導管2 5供應的吸收液體）。 物流10 實例1 實例2 實例 非依據本發明依據本發明 依據本發明
上述結果說明了將回流物流分成兩個回流物流，亦即 i、應至洗滌塔6頂部的第一回流物流以及供應至汽提區段 7頂部的第二回流物流，以回收天然氣液態物質的有利效 果。 依據本發明之方法可用以從天然氣中移除較重成份， 此天然氣在處理之後被導入用來將氣體輸送至使用者的導 管0 μ而，依據本發明之方法可適當地用以從天然氣中移 除較重之成分’該天然氣在處理之後被供應至使天然氣液 化之工廠。 【圖式簡單說明】 圖1為本發明第一具體實例之流程圖；以及 圖2為本發明第二具體實例之流程圖。 21 1313186 【元件符號】 1 導管 2 熱交換器 3 導管 6 洗；:條塔 7 汽提區段 8 吸收區段 9 間隔 10 導管 12 導管 14 熱交換器 17 分離容器 20 導管 21 導管 22 導管 23 導管 25 導管 30 汽提塔 33 汽提區段 34 減低壓力閥 35 導管 36 再沸器 38 導管 40 導管 22 1313186 43 熱交換器 46 分離器 48 導管 50 導管 53 壓縮器 55 熱交換器 57 熱交換器 23

Claims (1)

1313186 拾、申請專利範圍： 1 ·—種於提高壓力下從氣態天然氣物流中移除天然氣 液態物質以獲得具有減少含量之天然氣液態物質之氣態產 物流的方法，此方法包括以下步驟： (a) 將該天然氣物流冷卻； (b) 將冷卻的天然氣物流導入具有下汽提區段及上吸收 區·^又的洗滌k之底部，每一區段含有至少一個理論階； (c) 使天然氣通過洗滌塔上升，並從洗滌塔頂部移除 塔頂物流； (d) 部分冷凝此塔頂物流，及將此部分冷凝的塔頂物 流分離成具有減少含量之天然氣液態物質的氣態物流以及 液態回流物流’並將此氣態物流以具有減少含量之天然氣 液態物質之氣態產物流移除； (e) 將液態回流物流分成第一回流物流與第二回流物 流； (f) 將苐一回流物流導入洗務塔的吸收區段之頂部； (g) 將第二回流物流導入汽提區段的頂部，以汽提所 要的輕質氣態成份；以及 (h) 從洗滌塔底部移除富含較重成份的液態塔底物流 〇 2.如申請專利範圍第1項之方法’其中於步驟（句中之 部分冷凝該塔頂物流是藉由與至少部分的氣態產物流間接 熱交換而冷卻。 3 .如申請專利範圍第1項之方法’其更包含將該液雜 24 1313186 塔底物流於較低壓力下導入具有至少一個理論分離階的汽 提塔之頂部；從該汽提塔底部移除有一部分被汽化的液態 物流’該部分被導入汽提塔之底部；從該汽提塔頂部移除 氣態塔頂物流；部分冷凝該氣態塔頂物流並將該部分冷凝 的塔頂物流分成液態餾份與氣態餾份；將該液態餾份導入 該汽提塔的頂部；以及將該氣態塔頂餾份加入該氣態產物 流。 长4·如申請專利範圍第3項之方法，其中該氣態塔頂物 流係藉由與該氣態產物流間接熱交換而部分冷凝。 5 ·如申π專利範圍第3項之方法，其中來自該洗滌塔 的液態i合底物流係藉由與該氣態產物流間接熱交換而冷卻 / 如申請專利範圍f i至5項中任一項之方法，其中 該天然氣物流係藉由與該氣態產物流間接熱交換而部分冷 凝。 人7.如申請專利範圍帛1項之方法，其更包含將碳氩化 合物液體導入該吸收區段的頂部。 8·如申請專利範圍第…項中任—項之方法，其更 。3將碳氫化合物液體導人該吸收區段的頂部。 =中請專利範㈣8項之方法，其中該碳氫化合物 液體係藉由與該氣態塔頂餘份間接熱交換而冷卻。 10. —種液化天然氣的 r m ^ λ 方法，該方法包括根據申請專利 辄圍弟1至8項中任— 中移除天然氣液態物f，法來從氣態天然氣物流 乂獲得具有減少含量之天然氣液 25 -1313186 ψ 態物質之氣態產物流，以及使該氣態產物流液化以獲得液 化天然氣。 拾壹、圖式： 如次頁。 26 1313186 柒、指定代表圖： (一） 本案指定代表圖為：第（1 )圖。 (二) 本代表圖之元件代表符號簡單說明： 捌、本案若有化學式時，請揭示最能顯示發明特徵的化學式： 1 導管 2 熱交換器 3 導管 6 洗滌塔 7 汽提區段 8 吸收區段 9 間隔 10 導管 12 導管 14 熱交換器 17 分離容器 20 導管 21 導管 22 導管 23 導管 25 導管
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