CN1747775A - 从气态天然气物流中脱除天然气液体 - Google Patents

从气态天然气物流中脱除天然气液体 Download PDF

Info

Publication number
CN1747775A
CN1747775A CNA2004800038836A CN200480003883A CN1747775A CN 1747775 A CN1747775 A CN 1747775A CN A2004800038836 A CNA2004800038836 A CN A2004800038836A CN 200480003883 A CN200480003883 A CN 200480003883A CN 1747775 A CN1747775 A CN 1747775A
Authority
CN
China
Prior art keywords
stream
natural gas
gaseous
liquid
overhead
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CNA2004800038836A
Other languages
English (en)
Other versions
CN100381195C (zh
Inventor
E·C·布拉斯
P·S·库马
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of CN1747775A publication Critical patent/CN1747775A/zh
Application granted granted Critical
Publication of CN100381195C publication Critical patent/CN100381195C/zh
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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

Landscapes

  • 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)

Abstract

在提高压力下从气态天然气物流中脱除天然气液体，以获得天然气液体含量降低的气态产品物流的方法，包括：(a)将冷却的天然气(3)导入由下部汽提段(7)与上部吸收段(8)组成的洗涤塔(6)；(b)从洗涤塔脱除塔顶物流(12)；(c)部分冷凝(14)塔顶物流(12)，并将部分冷凝的塔顶物流分离(17)成气态产品物流(20)以及液态回流物流(21)；(d)将液态回流物流(21)分成第一回流物流(22)与第二回流物流(23)；(e)将第一回流物流(22)导入洗涤塔(6)的吸收段(8)顶部；和(f)将第二回流物流(23)导入汽提段(7)的顶部，并从洗涤塔(6)的底部脱除富含较重组分的液态塔底物流(10)。

Description

从气态天然气物流中脱除天然气液体
技术领域
本发明涉及从气态天然气物流中脱除天然气液体。在说明书与权利要求中，术语天然气液体是指称较重的烃如液化石油气组分与天然汽油。
背景技术
因为天然气液体具有经济价值且因为脱除天然气液体会降低天然气物流的热值，所以要将天然气液体脱除。
通过实例确定要从中脱除天然气液体的天然气物流的摩尔组成为：甲烷86摩尔％，乙烷6摩尔％，丙烷4摩尔％，丁烷以上1摩尔％，而其余量则由其它组分如氮气、二氧化碳和氦气组成。
本发明具体涉及在提高的压力如在大于3MPa(绝压)和小于天然气临界压力(约7MPa(绝压))的压力下从天然气物流中脱除天然气液体。
US 5325673公开了一种从天然气物流中脱除较重的烃的方法，其公开一种通过从中脱除较重烃而预先处理用于液化作用的天然气物流的方法，包括以下步骤：
a)将天然气进料物流导入具有上部富集段与下部汽提段的洗涤塔中；
b)将进料物流与导入塔的上部富集段的液态回流物流接触，以吸收进料物流中的C5 +烃；
c)回收含有C2-C4烃且具有小于约1ppm的C6 +烃浓度的塔顶蒸汽产品；
d)再沸塔下段内的部分液体，以从进料物流中汽提出较轻的烃；
e)回收富含C5 +烃的液态塔底产品；和
f)操作塔以获得主要存在于塔顶产品中的C2-C4烃。
此已知方法针对的是获得具有很低C6 +烃浓度的塔顶产品，但该塔顶产品仍含有相当多的乙烷、丙烷与丁烷。
发明内容
本发明提供一种从气态天然气物流中脱除天然气液体的方法，其中达到高压分离，且具有高的丙烷回收率及高的甲烷和乙烷脱除率。此外，本发明的目的在于提供一种脱除天然气液体的方法，其中不需再沸器。
为达此目的，本发明提供一种在提高压力下从气态天然气物流中脱除天然气液体，以获得天然气液体含量降低的气态产品物流的方法，包括以下步骤：
(a)将天然气物流冷却；
(b)将冷却的天然气物流导入洗涤塔的底部，所述洗涤塔具有下部汽提段及上部吸收段，每一段含有至少一块理论板；
(c)使天然气上升通过洗涤塔，并从洗涤塔塔顶脱除塔顶物流；
(d)部分冷凝所述塔顶物流，及将所述部分冷凝的塔顶物流分离成天然气液体含量降低的气态物流及液态回流物流，并将所述气态物流作为天然气液体含量降低的气态产品物流脱除；
(e)将液态回流物流分成第一回流物流与第二回流物流；
(f)将第一回流物流导入洗涤塔的吸收段顶部；
(g)将第二回流物流导入汽提段顶部，以汽提出所要的轻质气态组分；和
(h)从洗涤塔塔底脱除富含较重组分的液态塔底物流。
适当地，本发明的方法还包含将烃液体导入吸收段顶部。
附图说明
现将通过实例参考附图更详细地说明本发明，其中
图1为本发明第一种实施方案的示意图；和
图2为本发明第二种实施方案的示意图。
具体实施方式
首先参照图1。将包含天然气液体(C2-C4烃C5 +烃)的气态天然气物流(其基本不含酸性气体)经由管线1供应至换热器2，该物流于换热器2中被部分冷凝。部分冷凝的天然气经由管线3供应至洗涤塔6的底部。进入洗涤塔的天然气压力介于约3-7MPa(绝压)之间，且温度介于0和-20℃之间。
洗涤塔6于供应天然气的压力下操作。洗涤塔6包含两段，即下部汽提区7以及通过间隔9与汽提区7隔开的上部吸收段8。汽提段7包含1-4块理论分离板，而吸收段8包含4-10块理论板。理论板可通过接触塔板或适当的填料来提供。
使天然气物流的气态馏分在洗涤塔6中上升通过汽提段7与吸收段8。天然气物流的液态馏分经由管线10从洗涤塔6脱除。
从洗涤塔6的顶部经由管线12脱除塔顶物流，该塔顶物流的天然气液体含量降低。该塔顶物流于换热器14中部分冷凝，并于分离容器17中分离成液态物流与气态产品物流。气态产品物流经由管线20移出分离容器17，并送至使气态产品物流液化的装置(未画出)。从管线21脱除液态物流。部分冷凝的塔顶物流的温度是介于-25℃至-65℃的范围内，且在部分冷凝的塔顶物流内的液体含量介于10-35摩尔％(以总塔顶物流为基准)之间。适当地，在将气态产品输送离开之前，可将从管线20脱除的气态产品物流供应至换热器14(未画出)，以提供用于部分冷凝塔顶物流的冷量。
经由管线22将部分液态物流作为第一回流物流导入洗涤塔6的顶部吸收段8的上方作为吸收剂。将此液体加到吸收段8中而与来自汽提段7的气体逆流接触。比甲烷更重的组分则被作为吸收剂的第一回流物流从气体中脱除。
将液态物流的剩余物作为第二回流物流经由管线23导入洗涤塔6内位于汽提段7上方的间隔9中。在汽提段7中，将第二回流物流和从吸收段8下降的液体与上升的天然气物流气态馏分逆流接触。气态馏分从液态物流中脱除轻质组分(甲烷和乙烷)。之后将具有低浓度轻质组分的液态物流经由管线10从洗涤塔6的底部脱除。
适当地，在管线23中第二回流物流的量为从分离容器17脱除的液态物流的10-95重量％之间。
另外，可将烃液体经由管线25导入吸收段8的顶部。适当的烃液体为丁烷。适当地，此附加吸收剂的量为经由管线22供应的液体量的1-4倍。适当地，此附加吸收剂由丁烷及丁烷以上组分所组成。
现参照图2。请注意，参考图1所讨论的元件将给予相同的符号，而将不在此讨论。将经由管线10脱除的液态塔底流导入汽提塔30的顶部，以从液态塔底物流中汽提出气态组分如甲烷和乙烷。汽提塔30具有包括至少一块理论分离板的汽提段33。汽提段33适当地包括2-10块理论分离板。在汽提塔30内的压力为介于2-3.5MPa(绝压)的范围。为了使液态塔底物流的压力减低，管线10包括压力减低阀34。
液态物流从汽提塔30底部经由管线35脱除。部分液态塔底物流于再沸器36内蒸发，并将所得蒸汽导入汽提塔30的底部。剩余物则经由管线38离开至储槽(未画出)或至另一个处理过程中(未画出)。
汽态塔顶物流从汽提塔30顶部经由管线40脱除。气态塔顶物流于换热器43内部分冷凝以获得部分冷凝的气态塔顶物流。于分离器46中将部分冷凝的塔顶物流分离成液态馏分与气态馏分。将液态馏分从管线48移出并作为回流导入汽提塔30的顶部。将气态馏分经由管线50移出并加入气态产品物流中。任选使用压缩机53将气态塔顶馏分的压力增加至气态产品物流的压力。
适当地，将经由管线20移出的至少部分气态产品物流供应至换热器14，以提供用于部分冷凝塔顶物流12的冷量。
适当地，气态塔顶馏分通过与经由管线20供应至换热器43的气态产品物流间接换热而部分冷凝。
适当地，经由管线10而从洗涤塔6脱除的液态塔底物流通过在换热器55内与气态产品物流间接换热而冷却。
于换热器2中，将管线1内的天然气物流部分冷凝，这一点适当地通过与气态产品物流间接换热而进行。
适当地，供应至洗涤塔6的烃液体在换热器57中通过与气态塔顶馏分间接换热而冷却。
现通过实例方式参考三组计算实例来描述本发明。于并非依据本发明的第一个实例中，仅将经由管线22的回流供应至洗涤塔6的顶部。于依据本发明的第二个实例中，经由管线22与23供应回流。而于依据本发明的第三个实例中，经由管线25供应附加的烃液体。选择每个实例中的操作条件以使天然气液体的回收最大化。
于所有实例中，洗涤塔含有八块理论分离板。于依据本发明的两个实例中，汽提段7含有二块理论分离板，而吸收段8含有六块理论分离板。
其结果概述于下表1-8中。
于表中，摩尔流量的单位为kmol/s，质量流量的单位为kg/s，温度的单位为℃，压力的单位为MPa(绝压)，而摩尔组成的单位为mol％。丁烷及丁烷以上组分为丁烷、异丁烷、戊烷、异戊烷、己烷以及庚烷。在组成中提及的其它组分为水、氮气、硫化氢、二氧化碳以及氦气。
表1  经由管线3供应的部分冷凝进料的数据
  物流3   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   7.90   7.55   7.73
  质量流量   155   142   145
  温度   0   -5   -5
  压力   5.6   5.8   6.0
  摩尔组成
  甲烷   0.862   0.882   0.882
  乙烷   0.064   0.062   0.062
  丙烷   0.042   0.036   0.036
  丁烷及丁烷以上组分   0.031   0.019   0.019
  其它组分   余量   余量   余量
表2  从洗涤塔顶部经由管线12脱除的塔顶物流的数据。请注意因为内部循环，其流量大于管线3内的流量。
  物流12   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   8.79   8.64   8.39
  质量流量   168   161   152
  温度   -19   -23   -18
  压力   5.6   5.6   6.0
  摩尔组成
  甲烷   0.852   0.871   0.897
  乙烷   0.080   0.078   0.070
  丙烷   0.064   0.043   0.022
  丁烷及丁烷以上组分   0.003   0.006   0.001
  其它组分   余量   余量   余量
表3  经由管线22供应至洗涤塔6顶部的回流的数据
  物流22   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   1.57   0.17   0.08
  质量流量   40.5   4.05   1.81
  温度   -43   -48   -54
  压力   5.6   5.8   6.0
  摩尔组成
  甲烷   0.571   0.650   0.720
  乙烷   0.176   0.170   0.155
  丙烷   0.241   0.152   0.078
  丁烷及丁烷以上组分   0.001   0.027   0.005
  其它组分   余量   余量   余量
表4  经由管线23供应至洗涤塔6汽提段7顶部的回流的数据
  物流23   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   不适用   1.54   1.46
  质量流量   不适用   3.68   3.31
  温度   不适用   -48   -54
  压力   不适用   5.8   6.0
  摩尔组成
  甲烷   不适用   0.650   0.720
  乙烷   不适用   0.170   0.155
  丙烷   不适用   0.152   0.078
  丁烷及丁烷以上组分   不适用   0.027   0.005
  其它组分   不适用   余量   余量
表5  经由管线25供应至洗涤塔6顶部的烃液体的数据
  物流25   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   不适用   不适用   0.12
  质量流量   不适用   不适用   7.9
  温度   不适用   不适用   -33
  压力   不适用   不适用   6.0
  摩尔组成
  甲烷   不适用   不适用   0.00
  乙烷   不适用   不适用   0.00
  丙烷   不适用   不适用   0.00
  丁烷及丁烷以上组分   不适用   不适用   1.00
  其它组分   不适用   不适用   0.00
表6  经管线20脱除的气态产品物流的数据
  物流20   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   7.196   6.927   6.852
  质量流量   128   120   109
  温度   -43   -49   -54
  压力   5.3   5.5   5.7
  摩尔组成
  甲烷   0.913   0.925   0.937
  乙烷   0.059   0.055   0.051
  丙烷   0.026   0.017   0.009
  丁烷及丁烷以上组分   0.0009   0.0011   0.0015
  其它组分   平衡   平衡   平衡
表7  从洗涤塔6底部经由管线10脱除的进料气体的液体馏分的数据
  物流10   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  摩尔流量   0.70   0.63   0.99
  质量流量   27   22   36
  温度   -2   -11   -10
  压力   5.6   5.8   6.0
  摩尔组成
  甲烷   0.343   0.401   0.401
  乙烷   0.108   0.133   0.133
  丙烷   0.208   0.255   0.218
  丁烷及丁烷以上组分   0.341   0.210   0.247
  其它组分   余量   余量   余量
通过比较从洗涤塔6底部经由管线10脱除的液态物流的烃含量，可将结果概述于表8中。
表8  经由管线10脱除的液态物流的组成，按经由管线1供应的进料组成的百分比计(考虑到最后一个实例中经由管线25供应的吸收液体)。
  物流10   实例1，非依据本发明   实例2，依据本发明   实例3，依据本发明
  甲烷   3.5   3.8   5.8
  乙烷   15   18   27
  丙烷   44   59   78
  丁烷及丁烷以上组分   97   93   94
上述结果说明了将回流物流分离成两个回流物流，即供应至洗涤塔6顶部的第一回流物流以及供应至汽提段7顶部的第二回流物流，对回收天然气液体具有有利效果。
本发明的方法可用于从天然气中脱除较重组分，此天然气在处理之后被导入用来将气体输送至用户的管线中。
但本发明方法可适当用于从天然气中脱除较重组分，该天然气在处理之后被供应至液化天然气的装置。

Claims (10)

1.一种在提高压力下从气态天然气物流中脱除天然气液体以获得天然气液体含量降低的气态产品物流的方法，此方法包括以下步骤：
a)将天然气物流冷却；
(b)将冷却的天然气物流导入洗涤塔的底部，所述洗涤塔具有下部汽提段及上部吸收段，每一段含有至少一块理论板；
(c)使天然气上升通过洗涤塔，并从洗涤塔塔顶脱除塔顶物流；
(d)部分冷凝所述塔顶物流，及将所述部分冷凝的塔顶物流分离成天然气液体含量降低的气态物流及液态回流物流，并将所述气态物流作为天然气液体含量降低的气态产品物流脱除；
(e)将液态回流物流分成第一回流物流与第二回流物流；
(f)将第一回流物流导入洗涤塔的吸收段顶部；
(g)将第二回流物流导入汽提段顶部，以汽提出所要的轻质气态组分；和
(h)从洗涤塔塔底脱除富含较重组分的液态塔底物流。
2.权利要求1的方法，其中于步骤(d)中部分冷凝塔顶物流通过与至少部分气态产品物流间接换热而冷却。
3.权利要求1或2的方法，还包含将所述液态塔底物流于低压下导入具有至少一块理论分离板的汽提塔顶部；从汽提塔底部脱除部分被蒸发的液态物流，所述被蒸发部分被导入汽提塔底部；从汽提塔顶部脱除气态塔顶物流；部分冷凝所述气态塔顶物流并将部分冷凝的塔顶物流分离成液态馏分与气态馏分；将液态馏分导入汽提塔顶部；和将气态塔顶馏分加入气态产品物流中。
4.权利要求3的方法，其中通过与所述气态产品物流间接换热而部分冷凝所述气态塔顶物流。
5.权利要求3或4的方法，其中通过与所述气态产品物流间接换热而冷却来自汽提塔的液态塔底物流。
6.权利要求1-5任一项的方法，其中通过与所述气态产品物流间接换热而部分冷凝所述天然气物流。
7.权利要求1的方法，还包含将烃液体导入所述吸收段顶部。
8.权利要求3-6任一项的方法，还包含将烃液体导入所述吸收段顶部。
9.权利要求8的方法，其中通过与所述气态塔顶馏分间接换热而冷却所述烃液体。
10.一种液化天然气的方法，该方法包括按照权利要求1-8任一项的方法从气态天然气物流中脱除天然气液体，获得天然气液体含量降低的气态产品物流，以及使所述气态产品物流液化获得液化天然气。
CNB2004800038836A 2003-02-10 2004-02-09 从气态天然气物流中脱除天然气液体 Expired - Fee Related CN100381195C (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP03250826 2003-02-10
EP03250826.9 2003-02-10

Publications (2)

Publication Number Publication Date
CN1747775A true CN1747775A (zh) 2006-03-15
CN100381195C CN100381195C (zh) 2008-04-16

Family

ID=32842840

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB2004800038836A Expired - Fee Related CN100381195C (zh) 2003-02-10 2004-02-09 从气态天然气物流中脱除天然气液体

Country Status (12)

Country Link
US (1) US7041156B2 (zh)
EP (1) EP1596963B1 (zh)
JP (1) JP4624343B2 (zh)
KR (1) KR101079553B1 (zh)
CN (1) CN100381195C (zh)
EA (1) EA007664B1 (zh)
EG (1) EG23807A (zh)
ES (1) ES2400810T3 (zh)
MY (1) MY136353A (zh)
NO (1) NO341163B1 (zh)
TW (1) TWI313186B (zh)
WO (1) WO2004069384A1 (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115183533A (zh) * 2022-06-10 2022-10-14 安徽万瑞冷电科技有限公司 一种氦气回收的深冷洗涤分离工艺

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7165423B2 (en) * 2004-08-27 2007-01-23 Amec Paragon, Inc. Process for extracting ethane and heavier hydrocarbons from LNG
EP1789739B1 (en) * 2004-09-14 2020-03-04 Exxonmobil Upstream Research Company Method of extracting ethane from liquefied natural gas
US20070012072A1 (en) * 2005-07-12 2007-01-18 Wesley Qualls Lng facility with integrated ngl extraction technology for enhanced ngl recovery and product flexibility
RU2446370C2 (ru) * 2006-06-16 2012-03-27 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ для обработки потока углеводородов и устройство для его осуществления
JP2010501657A (ja) * 2006-08-23 2010-01-21 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 炭化水素流の処理方法及び処理装置
AU2008270245B2 (en) * 2007-07-05 2011-03-24 Shell Internationale Research Maatschappij B.V. Method of removing liquid contaminant droplets from a gas stream, and wash tray
WO2009020473A1 (en) * 2007-08-09 2009-02-12 Fluor Technologies Corporation Configurations and methods for fuel gas treatment with total sulfur removal and olefin saturation
FR2943683B1 (fr) * 2009-03-25 2012-12-14 Technip France Procede de traitement d'un gaz naturel de charge pour obtenir un gaz naturel traite et une coupe d'hydrocarbures en c5+, et installation associee
US8262787B2 (en) * 2010-06-09 2012-09-11 Uop Llc Configuration of contacting zones in vapor liquid contacting apparatuses
US8635885B2 (en) 2010-10-15 2014-01-28 Fluor Technologies Corporation Configurations and methods of heating value control in LNG liquefaction plant
FR2971043B1 (fr) * 2011-01-31 2017-03-31 Ifp Energies Now Procede de liquefaction d'un gaz naturel a haute pression avec un pretraitement utilisant un solvant
US10852060B2 (en) * 2011-04-08 2020-12-01 Pilot Energy Solutions, Llc Single-unit gas separation process having expanded, post-separation vent stream
US8620964B2 (en) * 2011-11-21 2013-12-31 Motorola Mobility Llc Ontology construction
US20140366577A1 (en) 2013-06-18 2014-12-18 Pioneer Energy Inc. Systems and methods for separating alkane gases with applications to raw natural gas processing and flare gas capture
US20160216030A1 (en) 2015-01-23 2016-07-28 Air Products And Chemicals, Inc. Separation of Heavy Hydrocarbons and NGLs from Natural Gas in Integration with Liquefaction of Natural Gas
CA2977793C (en) * 2015-02-24 2020-02-04 Ihi E&C International Corporation Method and apparatus for removing benzene contaminants from natural gas
US10520249B2 (en) 2016-01-22 2019-12-31 Encana Corporation Process and apparatus for processing a hydrocarbon gas stream
US11668522B2 (en) 2016-07-21 2023-06-06 Air Products And Chemicals, Inc. Heavy hydrocarbon removal system for lean natural gas liquefaction
AU2018239332B2 (en) * 2017-03-21 2023-06-15 Conocophillips Company Light oil reflux heavies removal process
JP7026490B2 (ja) * 2017-11-21 2022-02-28 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード Ｂｏｇ再凝縮装置およびそれを備えるｌｎｇ貯蔵システム。
EP4007881A1 (de) * 2019-08-02 2022-06-08 Linde GmbH Verfahren und anlage zur herstellung von flüssigerdgas

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5472203A (en) * 1977-11-21 1979-06-09 Air Prod & Chem Production of liquefied methane
US4445917A (en) * 1982-05-10 1984-05-01 Air Products And Chemicals, Inc. Process for liquefied natural gas
AU572890B2 (en) 1983-09-20 1988-05-19 Costain Petrocarbon Ltd. Separation of hydrocarbon mixtures
DE3528071A1 (de) * 1985-08-05 1987-02-05 Linde Ag Verfahren zur zerlegung eines kohlenwasserstoffgemisches
SU1468911A1 (ru) * 1987-03-23 1989-03-30 Всесоюзный Научно-Исследовательский И Проектный Институт По Переработке Газа Способ извлечени углеводородов С @ из углеводородного газа
US4726826A (en) * 1987-07-17 1988-02-23 The M. W. Kellogg Company Method for partial condensation of hydrocarbon gas mixtures
DE3814294A1 (de) * 1988-04-28 1989-11-09 Linde Ag Verfahren zur abtrennung von kohlenwasserstoffen
US5325673A (en) 1993-02-23 1994-07-05 The M. W. Kellogg Company Natural gas liquefaction pretreatment process
JP3769043B2 (ja) * 1994-12-19 2006-04-19 日揮株式会社 炭化水素含有ガスの処理方法
RU2144556C1 (ru) * 1995-06-07 2000-01-20 Элкор Корпорейшн Способ разделения газового потока и устройство для его осуществления (варианты)
FR2739917B1 (fr) * 1995-10-11 2001-08-24 Inst Francais Du Petrole Procede et dispositif de fractionnement d'un fluide contenant plusieurs constituants separables,tel qu'un gaz naturel
FR2743083B1 (fr) * 1995-12-28 1998-01-30 Inst Francais Du Petrole Procede de deshydratation, de desacidification et de degazolinage d'un gaz naturel, utilisant un melange de solvants
JP3761960B2 (ja) * 1996-03-19 2006-03-29 仁美 鈴木 ガス中の二酸化炭素の除去方法
US5724833A (en) * 1996-12-12 1998-03-10 Phillips Petroleum Company Control scheme for cryogenic condensation
US6712880B2 (en) * 2001-03-01 2004-03-30 Abb Lummus Global, Inc. Cryogenic process utilizing high pressure absorber column

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115183533A (zh) * 2022-06-10 2022-10-14 安徽万瑞冷电科技有限公司 一种氦气回收的深冷洗涤分离工艺

Also Published As

Publication number Publication date
EG23807A (en) 2007-09-04
KR20050102102A (ko) 2005-10-25
NO20054193L (no) 2005-10-11
NO341163B1 (no) 2017-09-04
TWI313186B (en) 2009-08-11
ES2400810T3 (es) 2013-04-12
EP1596963A1 (en) 2005-11-23
US20040200353A1 (en) 2004-10-14
WO2004069384A1 (en) 2004-08-19
EA007664B1 (ru) 2006-12-29
CN100381195C (zh) 2008-04-16
US7041156B2 (en) 2006-05-09
JP4624343B2 (ja) 2011-02-02
NO20054193D0 (no) 2005-09-09
EA200501273A1 (ru) 2006-02-24
KR101079553B1 (ko) 2011-11-04
AU2004210442A1 (en) 2004-08-19
TW200505548A (en) 2005-02-16
JP2006517249A (ja) 2006-07-20
MY136353A (en) 2008-09-30
EP1596963B1 (en) 2013-02-20

Similar Documents

Publication Publication Date Title
CN1747775A (zh) 从气态天然气物流中脱除天然气液体
CN1715260A (zh) 低压烯烃回收方法
US8618344B2 (en) Process for recovery of propylene and LPG from FCC fuel gas using stripped main column overhead distillate as absorber oil
CN1305551C (zh) 分离多元气体混合物的吸收－水合耦合方法
CN1195717C (zh) 从含有烃类的混合气中分离回收乙烯、乙烷、丙烯和氢气的方法
EP4053251A1 (en) Method and device for recovering c2-c4 components in methane-containing industrial gas
CN1537667A (zh) 利用水合物法分离低沸点气体混合物方法及其系统
CN1085645C (zh) 包括两个补充溶剂再生步骤的气体脱水和脱气油的方法
CN1154829C (zh) 精馏的回流脱乙烷塔
CN1407304A (zh) 一种改进的轻烃深冷分离方法
CN111393250B (zh) 一种轻烃分离装置及方法
CN111393252B (zh) 一种轻烃分离装置及方法
CN104964517B (zh) 一种石油伴生气回收lng/lpg/ngl产品的超低温中低压脱氮方法
CN113354502B (zh) 一种组合吸收回收分离非饱和干气中低碳烃的方法
CN1310856C (zh) 从烯烃－氢混合物中分离烯烃和氢的方法
CN113354501B (zh) 一种组合式吸收法回收催化富气中c1、c2和c3的分离方法
CN111394120B (zh) 一种轻烃回收方法及装置
CN112138421B (zh) 一种油气处理装置及方法
CN113354506A (zh) 一种组合吸收回收分离炼厂饱和干气中低碳烃的方法
CN101067092A (zh) 一种煤焦油加氢转化过程低分油的分离方法
CN111056904A (zh) 一种回收炼厂焦化装置干气中各种有效组分的方法
CN112521968B (zh) 一种轻烃回收方法及装置
CN1025628C (zh) 加氢裂化装置c3、c4烃的回收方法
CN112011356B (zh) 一种轻烃分离回收液化气的装置及方法
CN112760126B (zh) 一种油气分离及回收的装置和方法

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20080416

Termination date: 20160209

CF01 Termination of patent right due to non-payment of annual fee