CN108431184B - 在气体减压站制备天然气以生产液体天然气(lng)的方法 - Google Patents

在气体减压站制备天然气以生产液体天然气(lng)的方法 Download PDF

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CN108431184B
CN108431184B CN201580084284.XA CN201580084284A CN108431184B CN 108431184 B CN108431184 B CN 108431184B CN 201580084284 A CN201580084284 A CN 201580084284A CN 108431184 B CN108431184 B CN 108431184B
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methanol
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CN108431184A (zh
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J·洛伦索
M·米利亚尔
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1304342 Alberta Ltd
1304338 Alberta Ltd
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Abstract

在气体减压站预处理入口天然气流以生产LNG的方法，从天然气流中去除水和二氧化碳。所述方法所需的能量通过回收所述入口气流中的压力能来提供。所述方法避免了采用气体燃烧加热器的减压站的常规气体预加热方法。所述方法提供了在天然气减压站生产满足产品规格的LNG的方法。

Description

在气体减压站制备天然气以生产液体天然气(LNG)的方法
技术领域
本发明涉及通过回收从输送管线至分配管线的压力降低，而在气体减压站制备用于生产LNG的天然气的方法。回收的压力能被转换成电能和制冷能以制备和生产LNG。
在一个实例中，为了制备用于生产LNG的天然气，天然气流中的水和二氧化碳含量被降低以满足LNG产品规格，并且甲醇流在减压站通过回收的气体压力能进行调节，用以从天然气流中去除水和二氧化碳。
背景技术
减压站沿着用于向区域管线分配气体的高压天然气主输送管线设置。减压站的目的是控制天然气至区域分配管线的流动和压力。当气体压力减小时，温度也降低，这被称为焦耳-汤普森(Joules-Thompson)效应。温度降低的程度取决于压差和用于减小压力的设备。当所用的设备是减压阀时，每改变1个大气压，温度降低约0.5℃。当所用的设备是气体膨胀器涡轮时，每改变1个大气压，温度降低高达2℃。气体温度的这种降低可由于天然气流中的水含量而产生水合物，需要在压力减小之前对气体进行调节以防止水合物的形成。
现有减压站的通常做法是使用减压阀，因为它产生较低的温度降低。为了调节气体并防止水合物的形成，在压力减小之前，将气体预加热至确保减压后气体高于0℃的温度。
这些站的典型减压可消耗其至区域分配管线的气流通量的高达1.5％，以预加热气体并防止水合物的形成。
LNG的生产通常在位于气体输送管线不可用和或不经济的区域中的大型装置中进行。LNG通过将其作为液体装运至港口，为天然气生产商提供了管线运输的替代方案。在这些大型装置制备和生产LNG的气体工艺需要大量的能量输入，其主要目的是将其运输至港口，在那里其被再气化并通过高压输送管线以气相运输至市场。最近，天然气工业开始推广使用LNG作为柴油的替代燃料，主要是货运行业的替代燃料。所述工作面临的主要挑战是缺乏生产、储存和向消费者分配LNG的基础结构。目前LNG的主要供应通常被非常大量地递送至港口，这些港口可能远离市场，导致高分配成本。
在LNG的经济生产中的主要挑战是去除二氧化碳以满足LNG产品规格。在一些专用方法中，甲醇被用作溶剂。其它方法可基于由Lurgi开发的Rectisol和由IFP开发的Ifpexol。Rectisol方法主要用于合成的纯化中，以选择性地去除硫化氢，典型的工作温度是-40至-60℃。Ifpexol方法用于天然气处理应用中，以去除阶段1中的水和烃以及阶段2中的酸性气体，典型的操作温度是-20至-40℃。在这两种情况下，这些方法在工业中的使用都受到限制，这是由于其高资本和操作成本以满足对方法的甲醇制冷需要。
推广使用LNG作为柴油的替代品使得使用外部冷源(如液氮或制冷压缩循环)的小型LNG装置得以发展。典型的气体预处理通过使用分子筛去除水和二氧化碳来进行。分子筛是经过验证的商业化方法，但它们的资本和操作成本昂贵。
发明内容
根据一个方面，提供制备用于在减压站生产液化天然气(LNG)的天然气的方法。第一步骤涉及用甲醇预处理天然气流以吸收水馏分，之后在逆流热交换器中预冷却以冷凝并回收甲醇和水。第二步骤涉及在具有逆流制冷甲醇流的塔中进一步冷却天然气并汽提二氧化碳。第三步骤涉及在返回汽提塔之前通过逆流热交换对再生且循环的甲醇流进行制冷。第四步骤涉及将预冷却且预处理的天然气流分离成两个流：去往区域分配管线的天然气流和用于LNG生产的天然气流。第五步骤涉及通过气体膨胀器发生器将高压、预处理、预冷却的天然气流的压力减小至区域分配管线压力，以产生制冷能和电能。第六步骤涉及以逆流热交换将用于LNG生产的预处理、预冷却的高压天然气流进一步冷却，以冷凝并去除较重的烃馏分，由此将天然气流控制为LNG生产烃规格。第七步骤涉及在将天然气LNG产物流膨胀至LNG分离器压力之前，用来自LNG分离器的低温蒸气进一步冷却天然气LNG产物流以增加LNG产率。第八步骤涉及通过与以下物流的逆流热交换流动将去往区域分配管线的天然气流的温度升高：LNG生产流、去往汽提塔的再生甲醇流和去往减压站的入口气流，由此消除对于通过燃烧进行气体预加热的需要。
所述方法的目的是在减压站生产LNG而不使用外部能源，回收并使用输送管线压力能来生产LNG，以及消除通过燃烧预加热气体的做法。在减压站生产LNG提供了其在靠近使用点的分配。
所公开的方法涉及在气体减压站制备天然气。在一个优选的实施方案中，本方法制备用于生产LNG和电力的天然气，其包括：
(a)第一，通过剂量受控流动将甲醇注入到达气体减压站的连续流动的高压入口天然气流中。
(b)第二，将连续流动的入口天然气流预冷却，以冷凝、分离并收集甲醇、水和一些烃冷凝物。
(c)第三，在甲醇汽提塔中进一步冷却和预处理所述入口天然气流，以去除二氧化碳和残留痕量的水。
(d)第四，将甲醇、二氧化碳和一些烃冷凝物的甲醇汽提塔底部流混合物传送(routing)至甲醇再生塔。
(e)第五，将经预处理、预冷却的高压入口天然气流分离成两个流：去往区域分配管线的气体和用于LNG生产的气体。
(f)第六，通过气体膨胀器/发生器将去往区域分配管线的天然气流的高压减小至区域分配管线压力，以产生用于所述方法的制冷能和电能。
(g)第七，通过与以下物流的逆流流动进行热交换来回收去往区域分配管线的气流中产生的制冷能：用于LNG生产的气流、去往汽提塔的甲醇和减压站气体入口流。
(h)第八，通过来自LNG分离器的低温蒸气在逆流热交换器中进一步冷却LNG生产流。
(i)第九，通过膨胀器/发生器将高压气流LNG产物流减小至LNG分离器压力以产生LNG液体流和低温烃蒸气流。
(j)第十，将低温烃蒸气流与LNG生产流和减压站入口流传送于逆流热交换器中，以在将其压缩至区域气体分配管线压力之前回收所产生的制冷。
本发明所述的用于气体减压站的方法回收并使用输送气体管线压力能来生产LNG，并消除通过燃烧进行气体预加热的工业做法。
所述方法的一个主要特征是在减压站使用回收的能量来制冷甲醇，用于在满足LNG产品质量规格的气流的制备中有效地去除二氧化碳。
所述方法的另一特征是减压站从成本操作转换为收益操作。这种实用基础结构操作目前通过燃烧以一定成本预加热入口气体。所述方法消除了用于预加热的气体燃烧和其相关排放的做法，此外，它通过生产更高价值的商品LNG来产生收益。
如下文将描述的，上述方法可在任何天然气减压站操作以制备用于生产LNG的管线天然气流。
开发上述方法是为了在气体减压站制备和生产LNG。
如下文将进一步描述的，提供了一种LNG生产方法，其包括将高压的预处理、预冷却的天然气流分离成LNG生产流和区域分配管线流。去往区域分配管线流的预处理、预冷却的高压气体通过气体膨胀器/发生器减压以产生制冷气流和电力。LNG生产流进一步通过逆流热交换器利用去往区域分配管线的一部分制冷气流、之后是来自LNG分离器的低温烃蒸气冷却。然后，预处理、预冷却的LNG生产流通过第二气体膨胀器/发生器膨胀至LNG分离器中。所生产的液体馏分LNG被传送至储存器。低温烃蒸气馏分流的能量通过在压缩至区域气体分配管线之前将其传送至逆流热交换器中而被回收。
根据一个方面，提供在气体减压站生产液体天然气(LNG)的方法。气体减压站接收作为输入物的高压气体，并输出处于输出压力和温度范围的低压气体。所述方法包括以下步骤：
通过混合水合物抑制剂与所述高压气体的至少一部分来产生水合物抑制流；
通过以下方式产生脱水气流：
冷却所述水合物抑制流以产生液相，所述液相的至少一部分包含水，并将所述液相从所述水合物抑制流中分离出来；和
使用二氧化碳汽提剂去除二氧化碳；
冷凝所述脱水的气流以产生天然气的液体流和天然气的蒸气流；和输出作为所述低压气体的所述蒸气流。
根据另一方面，水合物抑制剂和二氧化碳汽提剂中的至少一种可以是甲醇。
根据另一方面，水合物抑制剂和二氧化碳汽提剂可以是甲醇，所述甲醇从所述脱水气流中回收，并且进一步包括通过从所述甲醇中分离水和二氧化碳来再循环所述甲醇的步骤。
根据另一方面，输出作为所述低压气体的所述蒸气流可包括调节所述温度和压力以落入所述输出压力和温度范围内。
根据另一方面，二氧化碳可被排放至大气中或输出至低压气体中。
根据一个方面，提供在气体减压站预处理和生产LNG的方法，其包括：
提供高压天然气流；
在热交换器中预冷却所述高压天然气流；
将甲醇注入所述高压天然气流中，并从所述高压天然气流中分离冷凝物，以在相分离器中产生脱水的天然气流；
使用溶剂膜从所述冷凝物中回收甲醇；
使所述脱水的天然气流通过二氧化碳汽提塔，以从所述脱水的天然气流中去除二氧化碳，以产生经处理的天然气流；
将所述经处理的天然气流分离成LNG生产流和分配流；
使用膨胀器/发生器降低所述分配流的所述气体压力，并从所述分配流中回收冷凝的烃馏分；
注入预冷却的甲醇流通过所述二氧化碳汽提塔，并从所述二氧化碳汽提塔中去除富甲醇流；
减小所述LNG生产流的所述温度和压力并从所述LNG产物流中回收液体烃馏分和气态馏分；
压缩并输出作为所述气体减压站的输出物的所述LNG分离器流的所述气态馏分；
通过从所述富甲醇流中去除所述二氧化碳而从所述富甲醇流中回收甲醇；和
冷却所述回收的甲醇，并将所述冷却的回收甲醇流分离成待注入所述高压天然气流中的第一甲醇流和待注入所述二氧化碳汽提塔中的第二甲醇流。
根据另一方面，所述高压气流可被在所述相分离器下游产生的低温预冷却。
根据另一方面，可采用热交换器在作为所述气体减压站的所述输出物输出之前预加热所述LNG分离器流的所述气态馏分。
根据另一方面，来自高压天然气流的冷凝物可包含水。
根据另一方面，二氧化碳汽提塔可以与制冷甲醇流逆流流动来去除二氧化碳。
根据另一方面，所述LNG生产流可在被冷凝为LNG之前被冷却以冷凝较重的烃馏分。
根据另一方面，回收的甲醇可使用在所述气体减压站回收的压力能被冷却。
根据下面的描述和附图将显而易见其它目的和方面。应当理解，可通过以任何合理的方式组合各种描述的元件来实现除了本文所述的那些之外的不同实施例。
附图简单说明
这些和其它特征将从下面参照附图的描述中变得更加显而易见，附图仅用于说明的目的，而不旨在以任何方式将本发明的范围限定于所示的一个或多个特定实施方案，其中：
图1是典型减压站的示意图，所述减压部装配有用于控制至区域分配管线的减压的JT阀、二醇/水加热器和二醇/水气体热交换器。
图2是LNG生产方法的示意图，所述方法被添加至现有气体降压站且装配有气体预处理单元、热交换器、汽提塔、气体膨胀器、KO鼓、泵和LNG储存器。方法天然气流由高压天然气输送管线供应。
图3是替代的LNG生产方法的示意图。
优选实施方案的详细描述
现在将参照图1至3描述该方法。
在本发明所述方法中，通过回收当前在减压站浪费的压力能来提供制冷能。回收的能量还允许甲醇在冷得多的温度下被制冷，并因此以更高的效率被制冷。例如，在本发明所述方法中，平均制冷甲醇温度是-80℃。
开发本方法是为了在气体减压站制备天然气流以生产LNG。所述方法以不同的方式使用甲烷膨胀循环，其迄今为止被用于被称为减压站的商业应用中。这里所述的系统在减压站利用递送至区域分配管线的气流，以提供在减压站生产LNG的改进方法。在一个实施例中，该方法预处理并去除水和二氧化碳，并且使用被从减压站入口处可用的输送管线压力回收的能量制冷的甲醇。所述方法在气体减压站产生并回收输送管线压力能，以对甲醇流进行制冷，并将其用作汽提塔中的二氧化碳汽提剂。在下面的描述中，
参照图1，天然气主输送管线的典型气体减压站。在理解操作原理后，本领域技术人员应当理解，使用已知的压力和温度设备进行变化是可能的。天然气从高压主输送管线递送，天然气流1通过截断阀2进入减压站并在热交换器3中预加热。预加热气流4的压力通过JT阀5减小至区域分配管线6的压力。区域分配管线6的压力由控制JT阀5天然气流动的压力变送器7维持。封闭再循环回路二醇/水11将来自加热器10的热量传递至气体热交换器3以预加热气体。温度变送器8通过控制流向二醇/水加热器10的气体流动流9来监测并控制区域气体分配管线温度。封闭回路再循环二醇/水11将来自加热器10的热量传递至气体热交换器3以预加热至减压站的入口气流。如图1中所示的这种简化的工艺布置构成了气体减压站的标准操作。在减压站降低压力之前预加热气体的目的是防止由于气体成分中存在水而形成水合物。
参照图2，所述方法显示为在现有减压站并行操作。如所描绘的，流1通过关闭减压截断阀2和打开阀13而被传送至LNG生产装置。天然气流14通过在线混合器15，其中添加甲醇流92作为水合物抑制剂以保持气体在液体溶液中的水含量。水合物抑制流16首先在热交换器17中被预冷却，并且进一步在热交换器19和21中被冷却，较冷的气流22进入气体/液体分离器23，其中水和甲醇通过流93被去除。蒸气馏分24被传送至二氧化碳汽提塔25，并与来自流76的制冷甲醇直接接触且逆流向上流动。二氧化碳汽提塔内件(internal)可以是鼓泡塔盘或填充床接触塔。制冷的甲醇从气体中汽提二氧化碳馏分并将其载送至塔的底部，并且通过料流77排出以进行再生。现在汽提出二氧化碳的天然气通过塔顶流26排出塔25。
大部分预处理的气体流26通过流47被传送至减压气体膨胀器/发生器48，其中排放的压力由区域气体分配管线压力连接器气流46控制。跨气体膨胀器/发生器48的压力减小产生电能并由于焦耳汤普森效应而降低流49的温度。较冷的气流49进入分离器50，其中冷凝物馏分51作为天然气液体被去除。气态流52是用于所述方法的主要制冷流。
经预处理的气态流27在热交换器54中进一步冷却，并且所得到的较冷气流28进入用于去除冷凝物的分离器29。热交换器54、之后的分离器29的目的是控制天然气流30的组成以满足LNG产品规格。较贫化的气流30在通过第二气体膨胀器/发生器35降低其压力之前在热交换器31和33中进一步冷却，从而产生更多电能。减压流36进入分离器37，在分离器37中液体天然气被分离并通过流38传送至储存器。低温气态流39通过管线39和40传送至热交换器33和19以回收其低温能，并通过气流41传送至压缩器42。压缩且加热的气流43被传送通过热交换器44(其中所述气流释放其压缩热)，并通过气流45传送至区域分配气体管线连接器流46。
天然气制冷流53通过热交换器54被流动控制，以提供针对流28中较重馏分冷凝的冷却要求，从而控制流30的气流组成。天然气制冷流55排出热交换器54且在热交换器56处提供进一步的制冷，作为流57排出，并且为了进一步制冷，与流68混合成流58，且进一步与流61混合成流62。
天然气制冷流59被传送通过热交换器60以控制进入二氧化碳汽提塔25的制冷甲醇流76的温度。制冷流61排出热交换器60并经由流58与天然气制冷流57和68混合，形成天然气制冷流62。天然气制冷流62进入热交换器21，之后经由管线63和64进入热交换器17，将其残留的制冷能释放给进入减压站的天然气流14。热回收气流65通过连接器流46被传送至区域气体分配管线6。这种热交换装置消除了通过气体燃烧在减压站预加热天然气的当前做法。
再生的甲醇流83被送至泵69并由环境空气翅片式风扇热交换器70预冷却。再生的预冷却甲醇流71被分离成流72和92。再生的甲醇流72在经由流76进入二氧化碳汽提塔25的顶部塔盘之前，经由流72、74和75在热交换器73、56和60中进一步冷却。制冷甲醇以与天然气逆流流动的方式沿塔向下流动，从天然气流中汽提二氧化碳馏分并作为富甲醇流77在塔底部排出，通过热交换器73以预冷却再生甲醇。预加热的富甲醇流78与富甲醇流96混合成富甲醇流79，通过减压阀80并通过流81进入甲醇再生塔82。再沸器流84被热交换器44加热以将来自甲醇的二氧化碳气化成流85。来自塔82的甲醇再生塔塔顶流86在进入分离器88之前由环境空气翅片式风扇热交换器87预冷却。回流流90通过泵89传送以控制塔82的塔顶温度。蒸气流91排出甲醇再生塔88，并通过连接器流46传送至区域气体分配管线6。再生的甲醇流92作为水合物抑制剂以受控剂量被传送至气体混合器15。流22的水合物抑制剂甲醇流馏分与天然气流中的水一起在分离器23处冷凝并回收。冷凝的混合物通过流93离开分离器23进入溶剂膜94中，在此处通过流95去除水流，回收的甲醇通过管线96传送至甲醇再生塔82中。
在所描绘的实施例中，所述方法使用减压气体入口流中的压力能来产生制冷流，该制冷流用于在气体减压站对甲醇流进行制冷以在CO2汽提塔中吸收并去除二氧化碳。在减压过程中使用膨胀器/发生器以产生焦耳汤普森效应是众所周知的，并且在气体工业中以各种形式实践。所提出的方法的优点是如下配置，即在减压站回收入口气流中的压力能以产生制冷气流，以对甲醇进行制冷以在汽提塔中汽提二氧化碳。
如应当理解的，图2中的实施方案是实施例，并且存在可用于实现类似结果的替代设计。例如，图3使用膜分离器100和111代替膨胀阀80、分离罐82和88以及如上文关于图2所述的其它设备，以将甲醇分离成流101和112，并将二氧化碳分离成流110和113。本领域技术人员将理解，可使用其它设备来实现与本文所述的类似的结果。
通常，减压站如图1中所示操作，需要使用一部分气流(通常为流入减压站的总入口气流的约1％)来预加热气体并防止水合物的形成。当使用所述方法时，可减少或消除燃烧气体用于气体预加热的需要以及在减压站使用工业标准分子筛技术用于从天然气流中去除CO2以生产LNG的需要。
在该专利文献中，词语“包含”在其非限制性意义上用于意指包括在该词语之后的项目，但不排除未具体提及的项目。不定冠词“一(a)”对要素的引用并不排除存在超过一种要素的可能性，除非上下文明确要求存在一种且只存在一种要素。
权利要求的范围不应受实施例中提出的优选实施方案限制，而是应当与作为整体的说明书一致地被给出宽泛的目的性解释。

Claims (7)

1.一种在气体减压站预处理和生产LNG的方法，其包含：
提供高压天然气流；
在热交换器中预冷却所述高压天然气流；
将甲醇注入所述高压天然气流中，并从所述高压天然气流中分离冷凝物，以在相分离器中产生脱水的天然气流；
使用溶剂膜从所述冷凝物中回收甲醇；
使所述脱水的天然气流通过二氧化碳汽提塔，以从所述脱水的天然气流中去除二氧化碳以产生经处理的天然气流；
将所述经处理的天然气流分成LNG生产流和分配流；
使用膨胀器/发生器降低所述分配流的所述气体压力，并从所述分配流中回收冷凝的烃馏分；
注入预冷却的甲醇流通过所述二氧化碳汽提塔，并从所述二氧化碳汽提塔中去除富甲醇流；
降低所述LNG生产流的温度和压力，并从LNG产物流中回收液体烃馏分和气态馏分；
压缩并输出作为所述气体减压站的输出物的LNG分离器流的所述气态馏分；
通过从所述富甲醇流中去除二氧化碳而从所述富甲醇流中回收甲醇；和
冷却所回收的甲醇，并将冷却的回收甲醇流分成待注入所述高压天然气流中的第一甲醇流和待注入所述二氧化碳汽提塔中的第二甲醇流。
2.根据权利要求1所述的方法，其中所述高压气流被在所述相分离器下游产生的低温预冷却。
3.根据权利要求1所述的方法，其中采用热交换器在作为所述气体减压站的所述输出物输出之前预加热所述LNG分离器流的所述气态馏分。
4.根据权利要求1所述的方法，其中来自所述高压天然气流的所述冷凝物包含水。
5.根据权利要求1所述的方法，其中所述二氧化碳汽提塔以与制冷甲醇流逆流流动来去除二氧化碳。
6.根据权利要求1所述的方法，其中所述LNG生产流在被冷凝为LNG之前被冷却以冷凝较重的烃馏分。
7.根据权利要求1所述的方法，其中使用在所述气体减压站回收的压力能冷却所回收的甲醇。
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