CN100516734C - 从液化天然气回收天然气液料的低温工艺 - Google Patents

从液化天然气回收天然气液料的低温工艺 Download PDF

Info

Publication number
CN100516734C
CN100516734C CNB2004800207336A CN200480020733A CN100516734C CN 100516734 C CN100516734 C CN 100516734C CN B2004800207336 A CNB2004800207336 A CN B2004800207336A CN 200480020733 A CN200480020733 A CN 200480020733A CN 100516734 C CN100516734 C CN 100516734C
Authority
CN
China
Prior art keywords
recovery tower
natural gas
liquefied natural
pressurization
heat exchange
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.)
Expired - Lifetime
Application number
CNB2004800207336A
Other languages
English (en)
Other versions
CN1826501A (zh
Inventor
斯科特·施罗德
肯尼思·雷迪克
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.)
Howe Baker Engineers LLC
Original Assignee
Howe Baker Engineers LLC
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 Howe Baker Engineers LLC filed Critical Howe Baker Engineers LLC
Publication of CN1826501A publication Critical patent/CN1826501A/zh
Application granted granted Critical
Publication of CN100516734C publication Critical patent/CN100516734C/zh
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • F25J3/0209—Natural gas or substitute natural gas
    • F25J3/0214—Liquefied 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
    • F25J3/0228—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
    • 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
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • 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
    • 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
    • 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
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (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
    • 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
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

披露了一种用于从液化天然气(LNG)回收天然气液料(NGL)(乙烷、乙烯、丙烷、丙烯和重碳氢化合物)的工艺。LNG进料流(1)被分流(22、23)，其中至少一部分用作不经过前处理的外部回流(23)，以改善天然气液料(NGL)的分离和回收。

Description

从液化天然气回收天然气液料的低温工艺
技术领域
本发明致力于比甲烷重的碳氢化合物从液化天然气(LNG)的回收，尤其涉及一种用于高产量回收比甲烷重的碳氢化合物、且同时利用最小外部供热来产生低BTU(British thermal unit，英国热量单位)液化天然气流的改进工艺。
背景技术
天然气一般包含最高达15％体积的比甲烷重的碳氢化合物。因此，一般分离天然气是为了提供管道品质气体部分(pipeline quality gaseous fraction)和较少挥发性液态碳氢化合物部分。这些重要的天然气液料(NGL)包括乙烷、丙烷、丁烷以及较少量的其它重碳氢化合物。在一些情况下，作为管道运输的一种替换方式，远距离处的天然气在特殊的LNG油罐中被液化并运输至适当的LNG处理和中转油库。随后，LNG被再次汽化并用作与天然气相同形式的气体燃料。因为LNG包含至少80摩尔百分比的甲烷，所以必须经常从较重的天然气碳氢化合物中分离甲烷以符合管道对热值的技术要求。另外，因为与作为燃料气体的价值相比，作为被用作石油化工原料的液态产品时NGL的组份具有更高的价值，故期望回收NGL。
一般通过包含“解吸油(lean oil)”吸附法、冷却“解吸油”吸附法以及低温凝结的许多公知工艺从LNG流回收NGL。尽管有许多熟知的工艺，但在高回收性和加工简易性(即，低投资支出)之间总存在一种折衷工艺。从LNG回收NGL的最普通的工艺是抽吸和汽化LNG，并随后将所得到的气体进行常用的工业标准涡轮膨胀型低温NGL回收加工。上述工艺需要在涡轮膨胀机或J.T.阀上具有大的压降以产生低温。另外，上述在先的工艺一般需要在LPG提取之后压缩所得到的气体，以获得预膨胀的步进压力(steppressure)。已经知晓该标准工艺的一些替换工艺并且在美国专利No.5,588,308和No.5,114,451中披露了两种这样的工艺。美国专利No.5,588,308中披露的NGL回收工艺利用自动制冷和综合热交换代替外部制冷或进料(feed)涡轮膨胀机。可是，该工艺要求LNG进料具有环境温度并被预处理以除去水、酸性气体及其它杂质。美国专利No.5,114,451中描述的工艺从LNG进料回收NGL，所述LNG进料已经通过与塔顶馏出物(fractionation overhead)的压缩循环部分进行热交换而被加热。压缩并加热包含富含甲烷的残余气的所述塔顶馏出物的其余部分，以便被引入管道分配系统。
本发明提供另一种可选的NGL回收工艺，该工艺产生低压的富含液态甲烷的流(stream)，其被引向主LNG出口泵(main LAG export pump)，其中该流能够被泵压至管道压力并最后发送至主要的LNG汽化器。另外，如以下说明书中所描述的以及之后权利要求所限定的，本发明将一部分LNG进料直接用作分离过程中的外部回流以获得高产量的NGL。本发明还提供所需成分和不需要成分之间的高度分离，进而减少过程中整体的燃料和能量消耗。
发明内容
如上所述，本发明涉及一种从LNG回收NGL的改进工艺，其避免了对脱水、去掉酸气和其它杂质的需要。该工艺的进一步优势是显著地减少了总的能量和燃料需求，因为实际消除了与一般NGL回收设备相关的残余气压缩的需求。该工艺还不需要涡轮膨胀机或J.T.阀上具有大的压降来产生低温。与一般的低温NGL回收设备相比，这减少了构成该工艺的30％-50％的资本投资。
本发明还在整个所述工艺中限制了LNG流的热增益，因而可提供附加的下游利益。通过最小化LNG的热增益，能够确保LNG在进入高压管道泵之前被完全液化并在泵的吸口处不存在蒸气。减少的热增益还使得可以在以低于设备容量的生产量运行该工艺的同时，在高压管道泵上游产生完全液化的LNG。另外，本发明的工艺允许我们使低BTU的LNG流快速进入储槽中，同时产生最小体积的蒸气。而且，本发明的工艺考虑到汽化蒸气(boil-offvapor)与低BTU的LNG混合的同时，仍在高压泵的上游产生完全汽化的LNG。
概括地说，我们的工艺通过在从重碳氢化合物液体分离富含甲烷流的过程中把从脱乙烷塔回收的塔顶产物用作回收塔的回流，利用低压液化天然气(例如直接来源于LNG存储系统)回收比甲烷重的碳氢化合物，从而产生高产量的NGL。在本发明中，回收塔的LNG进料流被加热至使该LNG进料流的一部分汽化，由此最小化供给脱乙烷塔的流体量(amount of fluid)以及脱乙烷塔所需的外部加热量，同时为较重的碳氢化合物的高产量的回收做准备。由分离步骤得到的富含甲烷的塔顶产物流被传送至低温、低压头压缩机的吸入侧，以便再液化该塔顶产物流。随后，该再液化的LNG与进料流进行交叉热交换并被引向主LNG出口泵。通过在被送至脱乙烷塔之前与脱乙烷塔塔顶产物的交叉热换热，回收塔的液态塔底产物被部分地汽化，以便进一步限制供给脱乙烷塔的外部加热量。
在本发明的替换方案中，来自于回收塔的富含甲烷的塔顶产物在与进料流进行交叉热交换之前得到冷却。本发明工艺的可能变化包括在放弃乙烷的同时回收丙烷和较重的碳氢化合物，或类似地执行这种任何期望的分子量的碳氢化合物的分离。在本发明工艺的一种可能变化中，丙烷回收处于90％至96％的范围内，并带有99+％的丁烷正回收(99+％butane-plus recovery)。
在本发明的替换方案中，通过给回收塔和/或脱乙烷塔提供回流流(refluxstream)或另加的进料流可以改变总的回收。在本发明的一个替换方案中，进入回收塔的LNG进料流被分成第一分流(split stream)和第二分流，所述第一分流在进入回收塔底部之前通过与压缩的回收塔塔顶产物流进行的交叉交换而被加热，所述第二分流直接被送入回收塔顶部。在本发明的另一替换实施例中，再液化的LNG流被分成排出到主LNG出口泵的第一分流，以及用作进入回收塔顶部的回流流的第二分流。在另一替换实施例中，来自于回收塔的塔底产物被压缩，随后，被分成第一分流和第二分流，所述第一分流在进入脱乙烷塔之前与来自于脱乙烷塔的塔顶产物流进行交叉热交换，所述第二分流被直接送至脱乙烷塔顶部。
本发明提供一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压的液态液化天然气分成第一和第二部分；
c)把步骤b)得到的加压液态液化天然气的第一部分引至冷却箱，其在所述冷却箱内被进行热交换以提高其温度；
d)把步骤b)得到的加压液态液化天然气的第二部分绕过所述冷却箱并将其作为第一回流引至回收塔；
e)把步骤c)得到的热交换后的加压液态液化天然气的第一部分引至回收塔，在所述回收塔中，通过结合所述第一回流和第二回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
f)加压所述回收塔塔底产物并使被加压的回收塔塔底产物与脱乙烷塔塔顶产物进行交叉热交换；
g)把交叉热交换后的回收塔塔底产物引至脱乙烷塔；
h)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
i)把交叉热交换后的脱乙烷塔塔顶产物作为所述第二回流引至所述回收塔；以及
j)从所述回收塔移除所述回收塔塔顶产物，并在引入所述冷却箱之前压缩该回收塔塔顶产物，以及与所述加压液体液化天然气的第一部分进行热交换以产生再液化的加压液化天然气。
本发明提供另一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压液态液化天然气引至冷却箱，在所述冷却箱中所述加压液态液化天然气被进行热交换以提高其温度；
c)把步骤b)得到的热交换后的加压液态液化天然气引至回收塔，在所述回收塔中，通过结合第一和第二回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
d)对所述回收塔塔底产物加压，并使加压的回收塔塔底产物与脱乙烷塔塔顶产物进行交叉热交换；
e)把交叉热交换后的加压回收塔塔底产物引至所述脱乙烷塔；
f)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
g)把热交换后的脱乙烷塔塔顶产物作为第二回流引至所述回收塔；
h)从所述回收塔移除所述回收塔塔顶产物，并在引入冷却箱之前压缩所述回收塔塔顶产物，以及与所述加压液态液化天然气进行热交换以产生再液化的加压液化天然气；以及
i)分离所述再液化的加压液化天然气的一部分以用作所述第一回流。
本发明还提供一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压液态液化天然气引至冷却箱，在所述冷却箱中，所述加压液态液化天然气被进行热交换以提高其温度；
c)把步骤b)得到的热交换后的加压液态液化天然气引至回收塔，在所述回收塔中，通过结合一回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
d)对所述回收塔塔底产物加压，并使加压的回收塔塔底产物与脱乙烷塔塔顶产物进行交叉热交换；
e)把交叉热交换后的加压回收塔塔底产物引至脱乙烷塔；
f)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
g)把热交换后的脱乙烷塔塔顶产物作为所述回流引至所述回收塔；以及
h)从所述回收塔移除所述回收塔塔顶产物，并在引入所述冷却箱之前压缩所述回收塔塔顶产物，以及与所述加压液态液化天然气进行热交换以产生再液化的加压液化天然气。
本发明还提供一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压液态液化天然气引至冷却箱，在所述冷却箱中，所述加压液态液化天然气被进行热交换以提高其温度；
c)把步骤b)得到的热交换后的加压液态液化天然气引至回收塔，在所述回收塔中，通过结合一回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
d)对所述回收塔塔底产物加压；
e)把所述加压的回收的塔底产物分成第一部分和第二部分；
f)把所述加压的回收塔塔底产物的第一部分与脱乙烷塔塔顶产物进行交叉热交换，并引导交叉热交换后的加压回收塔塔底产物引至脱乙烷塔；
g)在不进行热交换的情况下把所述加压回收塔塔底产物的第二部分作为回流引至所述脱乙烷塔；
h)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
i)把交叉热交换后的脱乙烷塔塔顶产物作为步骤c)所述的回流引至所述回收塔；以及
j)从所述回收塔移除所述回收塔塔顶产物，并在引入所述冷却箱之前压缩所述回收塔塔顶产物，以及与所述加压液态液化天然气进行热交换以产生再液化的加压液化天然气。
此外，在本发明的工艺中还可包括加热和再循环脱乙烷塔塔底产物的步骤。
附图说明
图1是本发明工艺的示意性流程图。
图2是本发明另一工艺的示意性流程图。
图3是本发明再一工艺的示意性流程图。
图4是本发明再一工艺的示意性流程图。
图5是本发明再一工艺的示意性流程图。
具体实施方式
从低压液化天然气(LNG)回收天然气液料(NGL)而不需要现有技术工艺中所使用的外部制冷或进料涡轮膨胀机。参照图1，示出了以极低的压力进入泵2的输入LNG进料流，其一般处于0-39.5kPa和低于-200°F的温度的范围内。泵2可以采用一般用于泵送LNG的任意泵设计方案，其被设定成能将LNG的压力从几百磅增加至接近790.8-3954.0kPa，优选为2372.4-2767.8kPa的变化范围。加热从泵2得到的流体流(stream)3，并通过在热交换器4中与流体流9中NGL自由残余气充分地进行交叉热交换而使其部分汽化。在加热和部分汽化之后，经热交换器4所产生的流体流5被送至回收塔6。回收塔6可以包括单一的分离工序或通常用于分离LNG进料的馏分(fractions)的几个单元操作的串流(series flow)布置。所用的具体(多个)回收塔的内部构造是常规工程设计的问题，其不限定本发明。
作为富含甲烷的流体流7的回收塔6的塔顶产物被移除并与NGL基本上分离。通过流体流来移除回收塔6的塔底产物，并且该塔底产物包括回收的NGL产物，其在该工艺的后点处被进一步分离以便移除乙烷。向低温低压头压缩机8的吸口传送流体流7中的甲烷富气塔顶产物(methane-rich gasoverhead)。需要压缩机8提供足够的压推力，使得排出的流体流9在主气体热交换器4中保持足够的温差，进而再液化富含甲烷的气体以形成再液化的富含甲烷的(LNG)排出流体流10。压缩机8用于实现大约517.1-792.9kPa的边际压力增加(marginal pressure increase)，压力优选地从大约2372.4kPa增加至大约2767.8-3360.9kPa。流体流10中再液化的LNG被引向主LNG出口泵(未示出)，在所述出口泵中液体将被泵压至管道压力并最后被传送至主要的LNG汽化器。
来自回收塔6的塔底产物11以处于-80至-170°F范围内的温度和具有689.5-3447.5kPa范围内的压力的情况进入泵12，所产生的加压流(pressurizedstream)13被供给热交换器14，在热交换器14中加压流13被加热至-100°F和0°F之间的温度。随后，将产生的加热流15传送至脱乙烷塔16。如果需要，可借助塔底重沸器或塔侧重沸器27来加热脱乙烷塔16。来自于脱乙烷塔16的塔顶产物流(overhead stream)17通过热交换器14，在热交换器14中塔顶产物流17用于加热被加压的回收塔塔底产物流(pressurized recoverytower bottoms stream)13。被冷却的脱乙烷塔塔顶产物流18用作回收塔6的回流流。移除脱乙烷塔塔底产物流19中比甲烷重的碳氢化合物。
在图2至5的说明中，相同的流体流和设备的参考标记用于指示与参照图1所述的设备和流体流成份相同的设备和流体流成份。
如图2所示，在本发明的可选实施例中，压缩机8排出的流体流9在冷却器20中冷却，并且所产生的预冷却的回收塔塔顶产物流21被供给热交换器4，在热交换器4中，所述塔顶产物流21与被加压的进料流3的进行交叉热交换。
在本发明的可选方案中，通过为回收塔6和/或脱乙烷塔16提供回流流或附加进料流来调节总回收。
图3示出了本发明的一个可选实施例，其中排出泵2的加压进料流3分别被分成第一分流22和第二分流23。第一分流22在底部进料流5进入回收塔6之前于热交换器4中与压缩的回收塔塔顶产物流9进行交叉热交换。第二分流23直接传送到回收塔6的顶部。
如图4所示，在本发明的另一可选方案中，来自于回收塔6的压缩并再液化的塔顶产物流10分别被分成第一分流24和第二分流25。第一分流24直接引到主出口泵(未示出)。第二分流25作为回流流被直接传送到回收塔6的顶部。
图5仍示出了本发明的另一方案，其中回收塔6的压缩塔塔底产物流13分别被分成第一分流26和第二分流28。第一分流26在热交换器14中与脱乙烷塔16的塔顶产物流17进行交叉热交换，并随后被送至脱乙烷塔16的顶部。第二分流28被直接传送到脱乙烷塔16的顶部。
热交换器、泵、压缩机以及回收塔的具体设计不应限定本发明；更确切地说，它是选择和判断特定的单元操作(unit operations)以获得所需性能的常规的工程实践问题。本发明致力于单元操作的独特组合以及将未处理的LNG用作外回流以实现高级别的分离效率进而回收NGL的新发现。
尽管已经描述了我们认定的本发明的优选实施例，但本领域的技术人员可意识到在不脱离以下权利要求所限定的本发明精神的情况下，可进行其它和进一步的改进，例如，将本发明用于各种条件、类型的进料或其它需求。

Claims (13)

1.一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压的液态液化天然气分成第一和第二部分；
c)把步骤b)得到的加压液态液化天然气的第一部分引至冷却箱，其在所述冷却箱内被进行热交换以提高其温度；
d)把步骤b)得到的加压液态液化天然气的第二部分绕过所述冷却箱并将其作为第一回流引至回收塔；
e)把步骤c)得到的热交换后的加压液态液化天然气的第一部分引至回收塔，在所述回收塔中，通过结合所述第一回流和第二回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
f)加压所述回收塔塔底产物并使被加压的回收塔塔底产物与脱乙烷塔塔顶产物进行交叉热交换；
g)把交叉热交换后的回收塔塔底产物引至脱乙烷塔；
h)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
i)把交叉热交换后的脱乙烷塔塔顶产物作为所述第二回流引至所述回收塔；以及
j)从所述回收塔移除所述回收塔塔顶产物，并在引入所述冷却箱之前压缩该回收塔塔顶产物，以及与所述加压液体液化天然气的第一部分进行热交换以产生再液化的加压液化天然气。
2.如权利要求1所述的工艺，其中，还包括加热和再循环所述脱乙烷塔塔底产物的步骤。
3.如权利要求1所述的工艺，其特征还在于，一汽化蒸气与所述回收塔塔顶产物相结合。
4.一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压液态液化天然气引至冷却箱，在所述冷却箱中所述加压液态液化天然气被进行热交换以提高其温度；
c)把步骤b)得到的热交换后的加压液态液化天然气引至回收塔，在所述回收塔中，通过结合第一和第二回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
d)对所述回收塔塔底产物加压，并使加压的回收塔塔底产物与脱乙烷塔塔顶产物进行交叉热交换；
e)把交叉热交换后的加压回收塔塔底产物引至所述脱乙烷塔；
f)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
g)把热交换后的脱乙烷塔塔顶产物作为第二回流引至所述回收塔；
h)从所述回收塔移除所述回收塔塔顶产物，并在引入冷却箱之前压缩所述回收塔塔顶产物，以及与所述加压液态液化天然气进行热交换以产生再液化的加压液化天然气；以及
i)分离所述再液化的加压液化天然气的一部分以用作所述第一回流。
5.如权利要求4所述的工艺，其中，还包括加热和再循环所述脱乙烷塔塔底产物的步骤。
6.如权利要求5的工艺，其特征还在于，所述被压缩的回收塔塔顶产物在引入所述冷却箱之前被预冷却。
7.如权利要求4所述的工艺，其特征还在于，一汽化蒸气与所述回收塔塔顶产物相结合。
8.一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压液态液化天然气引至冷却箱，在所述冷却箱中，所述加压液态液化天然气被进行热交换以提高其温度；
c)把步骤b)得到的热交换后的加压液态液化天然气引至回收塔，在所述回收塔中，通过结合一回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
d)对所述回收塔塔底产物加压，并使加压的回收塔塔底产物与脱乙烷塔塔顶产物进行交叉热交换；
e)把交叉热交换后的加压回收塔塔底产物引至脱乙烷塔；
f)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
g)把热交换后的脱乙烷塔塔顶产物作为所述回流引至所述回收塔；以及
h)从所述回收塔移除所述回收塔塔顶产物，并在引入所述冷却箱之前压缩所述回收塔塔顶产物，以及与所述加压液态液化天然气进行热交换以产生再液化的加压液化天然气。
9.如权利要求8所述的工艺，其中，还包括加热和再循环所述脱乙烷塔塔底产物的步骤。
10.如权利要求8所述的工艺，其特征还在于，汽化蒸气与所述回收塔塔顶产物相结合。
11.一种从液化天然气回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的液化天然气泵压至大于689.5kPa的压力；
b)把步骤a)得到的加压液态液化天然气引至冷却箱，在所述冷却箱中，所述加压液态液化天然气被进行热交换以提高其温度；
c)把步骤b)得到的热交换后的加压液态液化天然气引至回收塔，在所述回收塔中，通过结合一回流，回收塔塔顶产物随同回收塔塔底产物一起产生；
d)对所述回收塔塔底产物加压；
e)把所述加压的回收的塔底产物分成第一部分和第二部分；
f)把所述加压的回收塔塔底产物的第一部分与脱乙烷塔塔顶产物进行交叉热交换，并引导交叉热交换后的加压回收塔塔底产物引至脱乙烷塔；
g)在不进行热交换的情况下把所述加压回收塔塔底产物的第二部分作为回流引至所述脱乙烷塔；
h)移除作为脱乙烷塔塔底产物的比甲烷重的碳氢化合物；
i)把交叉热交换后的脱乙烷塔塔顶产物作为步骤c)所述的回流引至所述回收塔；以及
j)从所述回收塔移除所述回收塔塔顶产物，并在引入所述冷却箱之前压缩所述回收塔塔顶产物，以及与所述加压液态液化天然气进行热交换以产生再液化的加压液化天然气。
12.如权利要求11所述的工艺，其中，还包括加热和再循环所述脱乙烷塔塔底产物的步骤。
13.如权利要求11所述的工艺，其特征还在于，一汽化蒸气与所述回收塔塔顶产物相结合。
CNB2004800207336A 2003-07-07 2004-02-12 从液化天然气回收天然气液料的低温工艺 Expired - Lifetime CN100516734C (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US10/614,458 US6907752B2 (en) 2003-07-07 2003-07-07 Cryogenic liquid natural gas recovery process
US10/614,458 2003-07-07

Publications (2)

Publication Number Publication Date
CN1826501A CN1826501A (zh) 2006-08-30
CN100516734C true CN100516734C (zh) 2009-07-22

Family

ID=33564375

Family Applications (1)

Application Number Title Priority Date Filing Date
CNB2004800207336A Expired - Lifetime CN100516734C (zh) 2003-07-07 2004-02-12 从液化天然气回收天然气液料的低温工艺

Country Status (10)

Country Link
US (1) US6907752B2 (zh)
JP (1) JP4559420B2 (zh)
KR (1) KR100855073B1 (zh)
CN (1) CN100516734C (zh)
AU (1) AU2004263811B2 (zh)
BR (1) BRPI0412337A (zh)
CA (1) CA2531499C (zh)
GB (1) GB2418010B (zh)
MX (1) MXPA06000219A (zh)
WO (1) WO2005015100A1 (zh)

Families Citing this family (60)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6742358B2 (en) * 2001-06-08 2004-06-01 Elkcorp Natural gas liquefaction
US7475566B2 (en) * 2002-04-03 2009-01-13 Howe-Barker Engineers, Ltd. Liquid natural gas processing
US6907752B2 (en) 2003-07-07 2005-06-21 Howe-Baker Engineers, Ltd. Cryogenic liquid natural gas recovery process
US6986266B2 (en) * 2003-09-22 2006-01-17 Cryogenic Group, Inc. Process and apparatus for LNG enriching in methane
US7155931B2 (en) * 2003-09-30 2007-01-02 Ortloff Engineers, Ltd. Liquefied natural gas processing
US7278281B2 (en) * 2003-11-13 2007-10-09 Foster Wheeler Usa Corporation Method and apparatus for reducing C2 and C3 at LNG receiving terminals
CA2552245C (en) * 2004-01-16 2013-07-30 Aker Kvaerner, Inc. Gas conditioning process for the recovery of lpg/ngl (c2+) from lng
JP4452130B2 (ja) * 2004-04-05 2010-04-21 東洋エンジニアリング株式会社 液化天然ガスからの炭化水素分離方法および分離装置
US7204100B2 (en) * 2004-05-04 2007-04-17 Ortloff Engineers, Ltd. Natural gas liquefaction
EA010743B1 (ru) * 2004-06-30 2008-10-30 Флуор Текнолоджиз Корпорейшн Установка (варианты) и способ регазификации сжиженного природного газа
ES2284429T1 (es) * 2004-07-01 2007-11-16 Ortloff Engineers, Ltd Procesamiento de gas natural licuado.
US7207192B2 (en) * 2004-07-28 2007-04-24 Kellogg Brown & Root Llc Secondary deethanizer to debottleneck an ethylene plant
DE102005000634A1 (de) * 2005-01-03 2006-07-13 Linde Ag Verfahren zum Abtrennen einer C2+-reichen Fraktion aus LNG
JP5089173B2 (ja) * 2005-01-07 2012-12-05 独立行政法人理化学研究所 一塩基多型を用いた炎症性疾患の判定方法
GB0503213D0 (en) * 2005-02-16 2005-03-23 Bp Exploration Operating Process for conditioning liquefied natural gas
JP5411496B2 (ja) * 2005-03-22 2014-02-12 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 液化天然ガス流の希薄化方法及び装置
US20070012072A1 (en) * 2005-07-12 2007-01-18 Wesley Qualls Lng facility with integrated ngl extraction technology for enhanced ngl recovery and product flexibility
US10449736B2 (en) * 2006-02-02 2019-10-22 The Boeing Company Apparatus for fabricating thermoplastic composite parts
JP5198437B2 (ja) * 2006-05-23 2013-05-15 フルオー・テクノロジーズ・コーポレイシヨン Ｌｎｇ再ガス化設備における高エタン回収率の構成および方法
CA2653610C (en) * 2006-06-02 2012-11-27 Ortloff Engineers, Ltd. Liquefied natural gas processing
US9470452B2 (en) 2006-07-27 2016-10-18 Cosmodyne, LLC Imported LNG treatment
US7603867B2 (en) * 2006-09-11 2009-10-20 Cryogenic Group, Inc. Process and system to produce multiple distributable products from source, or imported LNG
US8499581B2 (en) * 2006-10-06 2013-08-06 Ihi E&C International Corporation Gas conditioning method and apparatus for the recovery of LPG/NGL(C2+) from LNG
US8820096B2 (en) 2007-02-12 2014-09-02 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and operation of the same
US9869510B2 (en) 2007-05-17 2018-01-16 Ortloff Engineers, Ltd. Liquefied natural gas processing
WO2009004794A1 (ja) * 2007-07-02 2009-01-08 Hitachi Metals, Ltd. Ｒ－Ｆｅ－Ｂ系希土類焼結磁石およびその製造方法
US20090199591A1 (en) 2008-02-11 2009-08-13 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Liquefied natural gas with butane and method of storing and processing the same
KR100954960B1 (ko) * 2008-02-28 2010-04-23 현대중공업 주식회사 해상 액화천연가스 생산설비의 초저온 미응축 가스 냉열회수장치
KR100929096B1 (ko) * 2008-03-14 2009-11-30 현대중공업 주식회사 연료가스 공급과 액화 천연가스 생산이 동시에 가능한 액화천연가스 생산 장치
KR100929097B1 (ko) * 2008-03-17 2009-11-30 현대중공업 주식회사 액화석유가스의 연료가스 공급용 예열장치와 액화천연가스생산용 예냉장치를 통합한 열교환기를 가지는 액화천연가스생산설비
KR100929095B1 (ko) * 2008-04-07 2009-11-30 현대중공업 주식회사 연료가스 공급과 액화 천연가스 생산이 동시에 가능한 액화천연가스 생산 장치
KR20090107805A (ko) 2008-04-10 2009-10-14 대우조선해양 주식회사 천연가스 발열량 저감방법 및 장치
US20090282865A1 (en) 2008-05-16 2009-11-19 Ortloff Engineers, Ltd. Liquefied Natural Gas and Hydrocarbon Gas Processing
WO2009143265A2 (en) * 2008-05-20 2009-11-26 Charles Neill Stripping of heavier hydrocarbons from liquefied natural gas
JP5688784B2 (ja) * 2008-07-31 2015-03-25 千代田化工建設株式会社 加熱モジュール
US8584488B2 (en) * 2008-08-06 2013-11-19 Ortloff Engineers, Ltd. Liquefied natural gas production
WO2010077614A2 (en) * 2008-12-08 2010-07-08 Howe-Baker Engineers, Ltd. Liquid natural gas processing
US8434325B2 (en) 2009-05-15 2013-05-07 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
US20100287982A1 (en) * 2009-05-15 2010-11-18 Ortloff Engineers, Ltd. Liquefied Natural Gas and Hydrocarbon Gas Processing
RU2554736C2 (ru) * 2009-07-21 2015-06-27 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ очистки многофазного углеводородного потока и предназначенная для этого установка
US20110067441A1 (en) * 2009-09-21 2011-03-24 Ortloff Engineers, Ltd. Hydrocarbon Gas Processing
US9021832B2 (en) * 2010-01-14 2015-05-05 Ortloff Engineers, Ltd. Hydrocarbon gas processing
IT1400370B1 (it) * 2010-05-31 2013-05-31 Nuova Pignone S R L Metodo e dispositivo per recuperare gas naturali liquefatti ngl
CN102933273B (zh) 2010-06-03 2015-05-13 奥特洛夫工程有限公司 碳氢化合物气体处理
US8635885B2 (en) * 2010-10-15 2014-01-28 Fluor Technologies Corporation Configurations and methods of heating value control in LNG liquefaction plant
KR101751830B1 (ko) * 2010-11-25 2017-06-28 대우조선해양 주식회사 천연가스 분류장치를 포함하는 부유식 해상 구조물
US20130213085A1 (en) * 2012-02-17 2013-08-22 Natural Gas Consultants LLC Hydrocarbon Mixture Processing System and Method using Vapor Recovery
CN105074370B (zh) * 2012-12-28 2017-04-19 林德工程北美股份有限公司 一种ngl(液化天然气回收)和lng(液化天然气)的组合工艺
JP5692709B2 (ja) * 2013-05-01 2015-04-01 千代田化工建設株式会社 冷却モジュール
CN104628505B (zh) * 2013-11-15 2016-09-07 中国石油天然气股份有限公司 一种从液化天然气中回收乙烷的方法及装置
US10808999B2 (en) * 2014-09-30 2020-10-20 Dow Global Technologies Llc Process for increasing ethylene and propylene yield from a propylene plant
CN104567275B (zh) * 2014-12-24 2016-08-24 四川科比科油气工程有限公司 一种高收率的天然气液化及轻烃回收装置及回收方法
AU2017249441B2 (en) 2016-04-11 2021-05-27 Geoff Rowe A system and method for liquefying production gas from a gas source
CA2971469C (en) 2016-06-13 2023-05-02 Geoff Rowe System, method and apparatus for the regeneration of nitrogen energy within a closed loop cryogenic system
US10551119B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10533794B2 (en) 2016-08-26 2020-01-14 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10551118B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US11543180B2 (en) 2017-06-01 2023-01-03 Uop Llc Hydrocarbon gas processing
US11428465B2 (en) 2017-06-01 2022-08-30 Uop Llc Hydrocarbon gas processing
US11585598B2 (en) * 2020-12-18 2023-02-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Operation of natural gas liquids stabilizer column

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3405530A (en) * 1966-09-23 1968-10-15 Exxon Research Engineering Co Regasification and separation of liquefied natural gas
US4689063A (en) * 1985-03-05 1987-08-25 Compagnie Francaise D'etudes Et De Construction "Technip" Process of fractionating gas feeds and apparatus for carrying out the said process
US5114451A (en) * 1990-03-12 1992-05-19 Elcor Corporation Liquefied natural gas processing
US5588308A (en) * 1995-08-21 1996-12-31 Air Products And Chemicals, Inc. Recompression cycle for recovery of natural gas liquids
US6311516B1 (en) * 2000-01-27 2001-11-06 Ronald D. Key Process and apparatus for C3 recovery
US6564579B1 (en) * 2002-05-13 2003-05-20 Black & Veatch Pritchard Inc. Method for vaporizing and recovery of natural gas liquids from liquefied natural gas

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1501013A (fr) * 1966-09-13 1967-11-10 Air Liquide Procédé de production d'un gaz riche en méthane, sous pression élevée à partirde gaz naturel liquide sous basse pression
US3837821A (en) 1969-06-30 1974-09-24 Air Liquide Elevating natural gas with reduced calorific value to distribution pressure
US5659109A (en) * 1996-06-04 1997-08-19 The M. W. Kellogg Company Method for removing mercaptans from LNG
US6510706B2 (en) * 2000-05-31 2003-01-28 Exxonmobil Upstream Research Company Process for NGL recovery from pressurized liquid natural gas
AU2001271587B2 (en) * 2000-08-11 2004-09-02 Fluor Technologies Corporation High propane recovery process and configurations
US6516631B1 (en) * 2001-08-10 2003-02-11 Mark A. Trebble Hydrocarbon gas processing
US6941771B2 (en) * 2002-04-03 2005-09-13 Howe-Baker Engineers, Ltd. Liquid natural gas processing
US6907752B2 (en) 2003-07-07 2005-06-21 Howe-Baker Engineers, Ltd. Cryogenic liquid natural gas recovery process

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3405530A (en) * 1966-09-23 1968-10-15 Exxon Research Engineering Co Regasification and separation of liquefied natural gas
US4689063A (en) * 1985-03-05 1987-08-25 Compagnie Francaise D'etudes Et De Construction "Technip" Process of fractionating gas feeds and apparatus for carrying out the said process
US5114451A (en) * 1990-03-12 1992-05-19 Elcor Corporation Liquefied natural gas processing
US5588308A (en) * 1995-08-21 1996-12-31 Air Products And Chemicals, Inc. Recompression cycle for recovery of natural gas liquids
US6311516B1 (en) * 2000-01-27 2001-11-06 Ronald D. Key Process and apparatus for C3 recovery
US6564579B1 (en) * 2002-05-13 2003-05-20 Black & Veatch Pritchard Inc. Method for vaporizing and recovery of natural gas liquids from liquefied natural gas

Also Published As

Publication number Publication date
GB2418010B (en) 2006-10-25
GB2418010A (en) 2006-03-15
WO2005015100A1 (en) 2005-02-17
US6907752B2 (en) 2005-06-21
CN1826501A (zh) 2006-08-30
AU2004263811A1 (en) 2005-02-17
KR100855073B1 (ko) 2008-08-29
AU2004263811B2 (en) 2008-05-08
CA2531499C (en) 2008-12-23
JP4559420B2 (ja) 2010-10-06
BRPI0412337A (pt) 2006-09-05
GB0526536D0 (en) 2006-02-08
US20050005636A1 (en) 2005-01-13
MXPA06000219A (es) 2006-03-21
JP2007527445A (ja) 2007-09-27
KR20060036441A (ko) 2006-04-28
CA2531499A1 (en) 2005-02-17

Similar Documents

Publication Publication Date Title
CN100516734C (zh) 从液化天然气回收天然气液料的低温工艺
CN101233376B (zh) 液化天然气加工方法
CN100445673C (zh) 用于液化高压天然气的系统和方法
US8110023B2 (en) Configurations and methods for offshore LNG regasification and BTU control
CN100417903C (zh) 低温天然气加工设施中用于液化天然气的方法和设备
CA2682684C (en) Configurations and methods for offshore lng regasification and heating value conditioning
CN102272544B (zh) 用于在lng液化设备中脱氮和/或回收氦气的方法
CA1097564A (en) Process for the recovery of ethane and heavier hydrocarbon components from methane-rich gases
AU2015231891B2 (en) Liquefied natural gas facility employing an optimized mixed refrigerant system
MX2007000929A (es) Reconfiguraciones y metodos de regasificacion de gas natural licuado.
CN105037069B (zh) 一种高压天然气的乙烷回收方法
JP2008534741A (ja) Ｌｎｇ再ガス化の精製および発電との統合
US20120096896A1 (en) Process for separating and recovering ethane and heavier hydrocarbons from LNG
CN105486034A (zh) 一种天然气液化与轻烃分离一体化集成工艺系统及工艺
US11408678B2 (en) Method and apparatus for separating hydrocarbons
CN100436988C (zh) 液化天然气的处理
CN205747680U (zh) 一种天然气液化与轻烃分离一体化集成工艺系统
US11274256B2 (en) Apparatus for separation and recovery of hydrocarbons from LNG
CN110590490B (zh) 一种回收液化天然气中烃类的系统和方法
US20090056371A1 (en) Method and Apparatus for Deriching a Stream of Liquefied Natural Gas
CN111108336B (zh) 天然气生产设备及天然气生产方法
MXPA04010908A (es) Procesamiento de gas natural liquido.

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
CX01 Expiry of patent term
CX01 Expiry of patent term

Granted publication date: 20090722