CN1826501A - 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

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CN1826501A
CN1826501A CNA2004800207336A CN200480020733A CN1826501A CN 1826501 A CN1826501 A CN 1826501A CN A2004800207336 A CNA2004800207336 A CN A2004800207336A CN 200480020733 A CN200480020733 A CN 200480020733A CN 1826501 A CN1826501 A CN 1826501A
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斯科特·施罗德
肯尼思·雷迪克
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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。
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，工艺100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0-5psig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100-500psig，优选为300-350psig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中与工艺100所排出的流体流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。利用工艺100通过流体流11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 gas overhead)。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75至115psi的边际压力增加(marginal pressure increase)，压力优选地从大约300psig增加至大约350-425psig。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100至500psia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。工艺100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分别被分成第一和第二分流22和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分别被分成第一和第二分流24和25。第一分流24通过工艺100而直接引到主出口泵(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分别被分成第一和第二分流26和27。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27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(LNG)回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的LNG泵压至大于100psia的压力；
b)把步骤a)得到的加压的液态LNG分成第一和第二部分；
c)把步骤b)得到的加压液态LNG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LNG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LNG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LNG的第一部分进行热交换以产生再液化的加压LNG。
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(LNG)回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的LNG泵压至大于100psia的压力；
b)把步骤a)得到的加压液态LNG引至冷却箱，在所述冷却箱中所述加压液态LNG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LNG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LNG的第一部分进行热交换以产生再液化的加压LNG；以及
i)分离所述再液化的加压LNG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3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。
7.一种从液化天然气(LNG)回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的LNG泵压至大于100psia的压力；
b)把步骤a)得到的加压液态LNG引至冷却箱，在所述冷却箱中，所述加压液态LNG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LNG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LNG的第一部分进行热交换以产生再液化的加压LNG。
8.如权利要求7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。
9.如权利要求5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。
10.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。
11.一种从液化天然气(LNG)回收比甲烷重的碳氢化合物的工艺，包括：
a)把液态、低压的LNG泵压至大于100psia的压力；
b)把步骤a)得到的加压液态LNG引至冷却箱，在所述冷却箱中，所述加压液态LNG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LNG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顶产物引至脱乙烷塔；
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所述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底产物，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LNG的第一部分进行热交换以产生再液化的加压LNG。
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8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。
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