CN101321985B - 气体在液态介质中大量运输和存储的方法 - Google Patents

气体在液态介质中大量运输和存储的方法 Download PDF

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CN101321985B
CN101321985B CN2006800248551A CN200680024855A CN101321985B CN 101321985 B CN101321985 B CN 101321985B CN 2006800248551 A CN2006800248551 A CN 2006800248551A CN 200680024855 A CN200680024855 A CN 200680024855A CN 101321985 B CN101321985 B CN 101321985B
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B·哈尔
M·J·穆尔瓦尼
T·奥基基奥卢
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Abstract

一种集成船装系统，该系统用于装载气流、分离重质烃、压缩气体、冷却气体、将气体与干燥剂混合、将气体与液态载体或溶剂调和，并将混合物冷却到处理、存储和运输条件。在将产品运输到目的地后，提供烃处理链和液体置换方法，以从管道和存储系统卸载液体，分离液体载体，并将气流输送到存储或运输系统。

Description

气体在液态介质中大量运输和存储的方法
技术领域
本发明通常涉及产出气或天然气或其它气体的存储和运输，特别涉及在液体介质中天然气、气相烃或其它气体的大量处理；还涉及将这些气体分离出一种气相以输送到存储或气体输送管路中。如本文所述，本发明特别适用于海上运输的轮船或驳船装置，并用于船上的气体处理，但同样可以用于陆地运输处理方式，如用于天然气的铁路、卡车和陆上存储系统。
背景技术
在轮船运输和高峰调节设备中，天然气主要以气态介质或以液化天然气(LNG)形式通过管道运输和处理。许多气藏远离市场，而且规模不到经济上值得通过管道或液化天然气(LNG)船运到市场的可开采天然气的规模。
由于船运压缩天然气(CNG)供应的天然气体积容量达到液化天然气(LNG)所供应的天然气比值600∶1的一半，使得船运压缩天然气慢慢商业化，这表明需要一种方法作为上述两种系统的补充。本文描述的方法的目的是满足两种系统之间存在的需求。
当产品输送到市场中心时，LNG系统的能耗强度通常需要采出气能量的10％到14％。在气体处理、气体压缩热、气体冷却以及后面的运输容器的排空方面，CNG需要更多的能量。如2004年8月26日递交的美国专利申请No.10/928757(757申请)所述，在此引入其内容以作参考，不采用低温条件储存，而在液化基质中处理天然气使其呈液态介质(称作压缩气液体TM(CGLTM)气体混合物)在此适合市场中具有其自身优点。在存储条件下从气相向液相压缩中，以及从运输系统卸载期间CGLTM气体混合物的100％置换中，CGLTM工艺都具有独特的能耗优势。
满足-40°F下1400psig存储条件的CGLTM工艺能量需求是适度的。在60°F到-20°F下，CNG的有效值(1800到3600psig)要求的较高压力，以及LNG(-260°F)需要的实际较低的低温会导致CNG和LNG工艺需要更多的能量。
因此需要提供能耗较低的便于存储和运输天然气或采出气的系统和方法。
概述
本发明的目的在于一种安装在海上运输船舶如轮船或驳船上的装置，用于装载产品气流、分离重质烃、压缩气体、冷却气体、用液态或固态干燥剂干燥气体、将气体与液态载体或溶剂混合，然后将混合物冷却到处理、存储和运输的条件。将产品运抵目的地后，提供烃加工链和液体置换方法，以从管道和存储系统卸载液体、分离液体载体，并将气流输送到典型的海岸存储或运输系统的储仓。
在一优选实施方案中，一独立的轮船或驳船包括加工、存储和运输系统，在该系统中采用乙烷、丙烷和丁烷的液态溶剂混合物，将天然气或气态烃转化成液化介质中，如757申请所述，溶剂的组成和体积根据工作条件和特定溶剂的有效性限度具体确定。此处处理链设计有：从船装管道系统卸载天然气产品或气态烃、分离和存储液态溶剂，以备下次装运重新使用。
本文描述的方法不限于轮船装置，也适用于运输介质上安装或没有安装处理链的其它运输形式。申请特别适用于现有容器的翻新，或用于新建轮船。
装载顺序优选从天然气或产品气从水下井口、FPSO(浮式采油)、海上平台或岸上管道流出，流经由浮桶或停泊码头直接或间接连接到轮船上的装载管道。气体流经一总管汇集至一个两相或三相分离器，以从气流中除掉游离水和重质烃。
该处理链为除去任何非理想组分以及洗涤器中的重质烃而使气流处于一定条件。然后气体被压缩、冷却、并被洗涤到接近存储压力-优选为约1100psig到1400psig。然后气体被用液态或固态干燥剂干燥，如甲醇-水混合物或分子筛，以控制水合物，然后在进入混合室之前与溶剂混合。得到的液态溶剂-气体混合物流通过冷冻系统被冷却到存储温度，约为-40°F。
气体进行脱水，以避免形成气体水合物。离开气体冷却器后，烃和水溶液分离以除去水相的组分，然后在存储条件下，新的干燥液体溶剂-气体混合物被装入存储管路系统。
存储产品保存在一排排的管束中、通过总管以上述方式相互连接，在这种形式下，每排中的物料可以选择分离或通过环状(looped)管系统再循环，该系统依次连接到冷冻系统，以在运输过程中持续保持存储温度。
卸载顺序包括管路系统中物料用甲醇-水混合物置换。存储的液态溶剂-气体混合物作为两相烃流进入脱乙烷塔之前，压力降低到约400psig的范围。主要由甲烷和乙烷组成的混合物从塔顶流出，在卸载管线中被压缩和冷却到传输管线特定的压力和温度。从脱乙烷塔底流出主要含丙烷和更重组分的物流，其进料到脱丙烷塔。
丙烷流从容器顶部回流到存储器，准备进行下一次气体运输，而富丁烷流从塔底泵送回在卸载管线中流动的甲烷/乙烷流中，以使气体的热值回归装载的产品流的热值标准。此工艺还能够调整销售气体的BTU值，以满足用户的BTU值要求。
通过验证下述附图和详细说明，本发明的其它系统、方法、特征和优点对本领域技术人员而言将是显而易见的。
附图说明
发明详细内容，包括构造、结构和操作，可以通过研究附图获取一部分，相同的附图标记表示相同的部件。附图中的部件没有必要按照比例，重点在于举例说明本发明的原理。另外，所有描述都是用于表达观念，其中的相对尺寸、形状和其它详细的属性可以是大略地说明，而不是逐字或精确说明。
图1是描绘本发明装载工艺的工艺流程图
图2是描绘顺序管组间置换工艺的工艺流程图。
图3是描绘本发明卸载工艺的工艺流程图
图4A是装有本发明集成系统的油轮的侧视图。
图4B和4C是显示安装在甲板上的装载和卸载系统的油轮的侧视图。
图5A是竖直排列管组的示意图
图5B是水平排列管组的示意图
图5C是另一种水平排列管组的示意图
具体实施方式
下面结合附图对本发明的细节进行说明，附图是示意图不是按比例的。仅仅用于举例，以下说明集中于轮船或海运。然而，本领域普通技术人员很容易认识到，本发明不限于此处描述的轮船或海运，同样还可以应用于陆上模式，如用于天然气的铁路、汽车和陆上存储系统。
在优选实施方案中，存储压力设置在低于2150psig，温度设置为低于-80°F。在这些优选压力和温度下，天然气和采出气在液体介质中的有效存储密度有利地超过了CNG的有效存储密度。为了降低能耗，优选的存储压力和温度是在约1400psig的范围，和约-40°F的范围。
如图4A所示，环状管道系统20，安装在油轮10的货舱30内，用来容纳运输的液化产品或天然气混合物。管道系统20被装在轮船或油轮10的绝热货舱30内。货舱30被含有冷冻惰性气氛14的绝热套12包裹，其中惰性气氛14在管路系统20中循环。在优选实施方案中，如图4B和4C所示，装载工艺装置100和分离、分馏以及卸载装置300被安装在油轮10的侧甲板上，以提供集成系统。
如图2B所示，管路系统20设计有竖直排列的管或管束22，管或管束22被设计为从位于管22侧面的顶部24或底部26开始使用。管22有无外套均可，优选安装包括顶侧24或底侧26的硬件，以最大程度使用竖直方向的空间。管道系统20的物料管22还优选包括通风孔和自由管基座，以最小化紧密包裹货舱的腐蚀和检查需要。
气体混合物的引入和排出优选经由带盖的管接头，作为管22的高液位；还经过到达管22的底部附近的带盖的汲取管(插入管)，作为管部分的低液位。这样做，以至使管中流体置换操作优选具有较高密度的产品从低液位引入，较低密度的产品从高液位移出。竖直汲取管优选用于填装、置换和循环工艺。
转到图5B和5C，提供了可替换的管道系统20，其中的管或管束22是水平排列的。如图5B所示，流体和气体从一端23流入，从另一端25流出。在图5C描述的实施方案中，流体和气体以螺旋形式流经管或管束22，而不是从23端流入，从25端流出。
参考图1，描述的是本发明的装载工艺100。油田产品流通过管道经由装油浮桶110收集，110是被船系缆的。装油浮桶110连接到通过缆索停泊的船上，其连接有软管。气流流向甲板上安装的进样分离器112，在此产生的水和重质烃分离并输送到不同部位。如果需要，主气流流向压缩系统114。产生的水从分离器112流向采出水处理装置116，其将水清洁到要求的环境标准。凝聚物从分离器112流向压缩气流。在存储罐118中单独存储凝聚物，或是被重新注入压缩气系统是可能的。
压缩系统114(如需要)将气体的压力提高到存储条件要求，优选条件是约1400psig和-40°F。压缩气在冷却器120中冷却，在洗涤器122中洗涤，然后被送到混合室124。从洗涤器122沉降的凝聚物被送到凝聚物存储罐118。
在混合室124中，气流与计量体积的天然气基液体(NGL)溶剂按申请757公开的参数进行混合，生成本文称为压缩气液体TM(CGLTM)气体混合物的气体-液体溶剂混合物。根据优选的储存参数，CGLTM气体混合物存储的压力范围是在约1100psig到约2150psig之间，温度优选范围是在约-20°F到约-180°F之间，更优选范围是在约-40°F到约-80°F之间。在制备CGLTM气体混合物中，采出气或天然气与溶剂混合，溶剂优选液态乙烷、丙烷或丁烷，或其混合物，以下面重量计算的浓度混合：乙烷优选约25％摩尔，优选范围在约15％摩尔到约30％摩尔之间；丙烷优选约20％摩尔，优选范围在约15％摩尔到约25％摩尔之间；或丁烷优选约15％摩尔，优选范围在约10％摩尔到约30％摩尔之间；或乙烷、丙烷和/或丁烷的混合物；或丙烷与丁烷的范围在约10％到约30％摩尔之间。
在冷却之前，CGLTM气体混合物优选用甲醇-水或固体干燥剂(如分子筛)进行脱水，以防止管系统130中形成水合物。NGL溶剂添加剂提供了适于存储更有效密度气体的环境，而干燥剂工艺为存储产品提供了脱水控制。
新的干燥气体/溶剂/甲醇混合物通过冷却器142，以单一相或两相液态流形式流出，其中冷却器142是冷冻系统的140的一部分，冷冻系统140包括压缩器144、冷却器146、收集器148和焦耳-汤姆逊阀149。然后此流流经分离器128，以从烃相中除去水相。水相返回甲醇再生和存储系统126。烃相流向主管道130，然后进入子管道，其中子管道向安装在竖直存储管束132顶部的总管进料。为了存储CGLTM气体混合物，优选引入到加压存储管道或容器束132中，132优选含甲醇-水混合物，以防止CGLTM气体混合物蒸发。
将CGLTM气体混合物引入管或容器束132优选采用竖直插管、竖直入口或出口线，从连接管132的盖133顶部总管的子管道流向管132的底135。管132填充、置换管道132中压力控制的甲醇-水混合物，直到安装在总管内的液位控制设备检测到CGLTM气体混合物，并使入口阀关闭。到入口阀关闭时，CGLTM气体混合物流转到填装下一个已经往复运送(shuttle)甲醇-水的管或容器束。
在循环的输送部分中，CGLTM气体混合物倾向于吸收一定的热量，从而温度稍微升高。当顶部总管上的温度传感器感应到较高温度时，管束常常将其物料经由循环泵138从顶部出口到小循环冷却装置136循环，从而使CGLTM气体混合物保持低温。一旦CGLTM气体混合物的温度达到优选的管道温度，冷却的CGLTM气体混合物循环到其它管束，并置换那些管束中温度较高的CGLTM气体混合物。
一种卸载工艺，其中CGLTM气体混合物在管道或容器束被置换，采出气或天然气被分离并卸载到市场管路，如图2和图3所示。存储的CGLTM气体混合物在管路系统220用存储在存储系统210中的甲醇-水混合物置换。此甲醇-水混合物经循环泵240泵送通过处理部分，以达到管路温度。如图2所示步骤1，冷的甲醇-水混合物从一个或一组管束222，如组1中，置换CGLTM气体混合物到图3所示的卸载装置。如步骤2所示，当甲醇-水混合物通过系统220卸压后，返回循环泵240以增大压力。然后高压甲醇-水混合物被关闭，以用于下一组管束222，如组2。通过降低流经减压阀310(图3)的置换流体的压力完成CGLTM置换。
如步骤2所示，甲醇-水混合物依次降低压力，并用如氮气的惰性(保护)气从管路系统220置换。如步骤3所示，甲醇-水混合物从管束222转走，填充气体留在管束222以便返航。
转到图3，根据卸载工艺300，其包括分离和分馏工艺，置换的CGLTM气体混合物从管路系统230流向压力控制站310，优选焦耳汤姆森阀，在此压力被降低。轻烃的两相混合物流向脱乙烷塔312，在此主要由甲烷和乙烷组成的塔顶流与重质组分，即丙烷、丁烷和其它重质组分分离。
从脱乙烷塔312底部离开的较重液体流流向脱丙烷塔314。脱丙烷塔314将丙烷馏分与丁烷和较重的烃馏分分离。丙烷馏分从塔顶流出，并在冷却器316中冷凝后送入回流罐318。一部分冷凝流作为回流从回流罐318送回脱丙烷塔314，其它的丙烷流向管路系统用作溶剂，并被存储在溶剂存储系统220中，重新用于下一批天然气或采出气的存储和运输。如图2步骤3所示，储备的各批NGL溶剂和甲醇-水混合物独立的保留在各组管束中，以用于待存储和运输天然气或采出气的下一次装载。
来自脱乙烷塔312的甲烷-乙烷气体流通过一系列热交换器(未示出)，在此气流的温度被提高。甲烷/乙烷气体流经压缩器324(如需要)后压力增加，然后通过流经冷却器326，甲烷/乙烷流的排出温度降低。
离开脱丙烷塔314底部的富丁烷流经过冷却器332，在此被冷却到常温，然后流向凝聚物存储罐334。
富丁烷流的旁流流经再沸器330，然后返回富丁烷流。丁烷凝聚物混合物通过泵336泵送到混合阀332，与溶剂的旁流汇合以调整BTU值，并最终与甲烷-乙烷流混合。气体混合物的总热含量优选调整到每1000立方英尺气体为950到1260BTU范围之间。
卸载气体很容易达到卸载到接受软管的输送条件，该接受软管与装油浮桶328相连。浮桶328再依次与陆地输送管路和存储装置连接。
在前述说明书中，已经参考特定其实施方案描述了本发明。然而，很明显，可以不脱离本发明精神和范围作各种修正。本领域技术人员熟知的特征和工艺可以根据需要进行添加和删减。因此，本发明不受附加权利要求和其等效内容的限制。

Claims (21)

1.一种用于天然气大量存储和运输的集成系统，包括：
装载和混合系统，适用于将天然气与选自乙烷、丙烷、丁烷或其混合物的液态溶剂混合形成液体介质形式的天然气-溶剂混合物，
容器系统，适用于在-40°F到-80°F的温度范围和在与天然气-溶剂混合物的天然气组分存储密度相关的存储压力下存储天然气-溶剂混合物，该存储密度超过了相同存储压力和温度下CNG的存储密度，和
分离、分馏和卸载系统，用于从天然气-溶剂混合物中分离出天然气。
2.权利要求1的系统，其中装载和混合系统，容器系统，和分离、分馏和卸载系统装配在运输容器上。
3.权利要求2的系统，其中运输容器是海上运输容器。
4.权利要求3的系统，其中运输容器是陆上运输容器。
5.权利要求1的系统，其中容器系统包括带保持温度和压力的循环装置的环状管道容器系统。
6.权利要求5的系统，其中环状管道系统包括水平嵌套管系统。
7.权利要求6的系统，其中水平嵌套管系统是为相邻管之间螺旋流体流动模式设计的。
8.权利要求5的系统，其中环状管道系统包括装配有竖直汲取管的竖直嵌套管系统，以集成装填、置换和循环功能。
9.权利要求8的系统，其中竖直嵌套管系统包括顶或底侧安装的硬件。
10.权利要求5的系统，其中环状管道系统包括通风口和配合用自由管基座。
11.权利要求1的系统，还包括在存储前脱水天然气的脱水装置。
12.权利要求11的系统，其中卸载系统包括从容器系统中置换天然气-溶剂混合物的置换装置。
13.权利要求12的系统，其中脱水和置换装置包括使用甲醇-水混合物作为脱水流体和置换流体。
14.权利要求13的系统，其中置换装置还包括用惰性气体吹扫置换流体的装置。
15.权利要求1的系统，其中卸载系统包括调整卸载的天然气的总热含量的装置。
16.权利要求15的系统，其中总热含量能波调整到每1000立方英尺天然气BTU值为950到1260的范围。
17.一种用于天然气大量存储和运输的方法，包括步骤：
将待运输天然气装载到运输容器上，
将天然气与选自乙烷、丙烷、丁烷或其混合物的液态溶剂混合，形成液体介质形式的天然气-溶剂混合物，
脱水所述天然气，
将用于运输的天然气-溶剂混合物存储在环状管道系统中，
循环存储的天然气-溶剂混合物，以维持预定的温度和压力。
从天然气-溶剂混合物中分离天然气，和
从运输容器卸载天然气。
18.权利要求17的方法，还包括在管道系统的管之间往复运送置换流体的步骤，以从管道系统置换天然气-溶剂混合物，来分离和卸载天然气。
19.权利要求17的方法，其中存储步骤包括在-20°F到-180°F温度范围内和1100psig到2150psig压力范围内存储天然气-溶剂混合物。
20.权利要求17的方法，还包括调整卸载的天然气的总热含量的步骤。
21.权利要求20的方法，其中总热含量能被调整到每1000立方英尺天然气BTU值在950到1260的范围。
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