CN1719169A - 富含碳氢化合物的气流的液化方法 - Google Patents

富含碳氢化合物的气流的液化方法 Download PDF

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CN1719169A
CN1719169A CN200510081887.2A CN200510081887A CN1719169A CN 1719169 A CN1719169 A CN 1719169A CN 200510081887 A CN200510081887 A CN 200510081887A CN 1719169 A CN1719169 A CN 1719169A
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hydrocarbon
mix refrigerant
circulation
flow
air
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海因茨·鲍尔
胡贝特·弗兰克
彭蒂·保罗拉
赖纳·扎佩尔
鲁道夫·施托克曼
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Linde GmbH
Equinor ASA
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Statoil ASA
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Abstract

提出了一种富含碳氢化合物的气流的液化方法，特别地一种天然气气流的液化方法；富含碳氢化合物的气流的液化通过包括两个混合制冷剂循环的混合制冷剂级联循环而发生，第一混合制冷剂循环被用于实现预冷却，第二混合制冷剂循环被用于实现将被液化的富含碳氢化合物的气流的液化和过冷却。根据本发明，第一混合制冷剂循环(1至12)被分离为低沸点气体部分(10)和高沸点液体部分(2)，并且两部分(2，10)以不同的压力被供应至预冷却部(E1)。

Description

富含碳氢化合物的气流的液化方法
技术领域
本发明涉及富含碳氢化合物的气流的液化方法，特别地涉及天然气气流的液化方法；富含碳氢化合物的气流的液化通过包括两个混合制冷剂循环的混合制冷剂级联循环(cascade cycle)而发生，第一混合制冷剂循环被用于实现预冷却，第二混合制冷剂循环被用于实现将被液化的富含碳氢化合物的气流的液化和过冷却。
背景技术
名词“预冷却”在下文应该被理解为将富含碳氢化合物的气流冷却到一个温度，在该温度，各重质或高沸点碳氢化合物发生分离。对将被液化的富含碳氢化合物的气流的随后的、进一步的冷却用名词“液化”来表示。
从德国专利申请197 22 490中可以知道所谓的单向流天然气液化方法。在该方法中，天然气气流的冷却、液化以及过冷却仅仅通过一个混合制冷剂循环而实现。压缩的混合制冷剂被部分地冷凝—优选地通过气体和冷却水，并被分离成低沸点气体部分(fraction)和高沸点液体部分。接着，这两部分以不同的压力级别被供应至用于冷却和液化将要被液化的天然气气流的一个或多个热交换器。
此单向流液化方法仅在生产能力最高为1mtpa的情况下才能经济性地操作。对于在1到5mtpa范围内的液化输出，通常使用所谓的双向流液化方法。
例如，从将要公开的德国专利申请10 2004 011 483中可以知道常见的双向流液化方法。然而，已经示出，尤其在从1到3mtpa相对小的生产能力范围内，已知的双向流液化方法需要改进。
通过引用上述两个德国专利申请，它们的公开内容被全部包括在本申请中。
发明内容
本发明的目的是提出一种将富含碳氢化合物的气流液化的通用方法，该方法可比已知的液化方法更加经济性地操作，特别地在相对小生产能力的上述范围内操作。
本发明的目的可通过一种通用液化方法来实现，该方法特征在于，第一混合制冷剂循环被分离为低沸点气体部分和高沸点液体部分，并且两个部分以不同的压力被供应至预冷却部。
附图说明
下面将参照附图中所示的实施方式来详细描述根据本发明的方法以及如从属权利要求中限定的其他各种实施方式。
图1是本发明的方法的流程图。
具体实施方式
如图1所示，将要被液化的富含碳氢化合物的气流经由管线a被供应至热交换器E1。在热交换器E1中，将要被液化的富含碳氢化合物的气流被冷却，直到容纳在其中的重质或高沸点碳氢化合物冷凝并可在分离单元H中与其分离；被处理的冷却气流经由管线b被供应至分离单元H。分离后的碳氢化合物经由管线c被排出，并且，可选地，被供应至进一步使用场所。
如果重质碳氢化合物容纳在将要被液化的天然气气流中，则通过预冷却、液化和排出，它们被分离为所谓的NGL(天然气液体)部分，并且如果其是可利用的，被供应至下一步处理阶段。富含碳氢化合物的气流或天然气中的将要被液化的成分—也就是C5+碳氢化合物和芳香族化合物，被称为重质或高沸点碳氢化合物；这些成分将在随后的冷却和液化中通过冷冻而分离出来。另外，将导致液化天然气的热卡值增加到不理想程度的碳氢化合物—特别地这里所提到的丙烷和丁烷，经常在液化之前被分离。
由于提供了所谓的HHC(重质碳氢化合物)萃取塔或涤气塔，其被用来从将要被液化的富含碳氢化合物的气流中分离出重质碳氢化合物和苯，因此通常可以实现高沸点碳氢化合物的分离。原则上，根据本发明的方法可与本领域目前所有已知的高沸点碳氢化合物分离方法结合。
富含碳氢化合物的气流(现已分离了高沸点碳氢化合物)，经由管线d被供应至第二热交换器E2，在第二热交换器E2内，富含碳氢化合物的气流通过第二混合制冷剂循环中的混合制冷剂被液化和过冷却。液化后的以及过冷却后的富含碳氢化合物的气流经由管线e从热交换器E2被排出，可选地在减压涡轮T1中被减压，并且接着被直接供应至进一步使用场所或经由阀f和管线g(暂时)储存起来。
根据本发明，通过(第一)混合制冷剂循环，执行热交换器E1中将要被液化的富含碳氢化合物的气流的预冷却。该(第一)混合制冷剂循环被分离为低沸点气体部分和高沸点液体部分，这两个部分以不同的压力被供应至热交换器E1。
出于此目的，经由管线5而从热交换器E1排出的混合制冷剂在双级压缩机V1的第一压缩级内被压缩至一个中间压力，通过热交换器E3中的环境空气或其他适合媒质其被部分冷凝，接着经由管线1被供应至第一分离器D。
高沸点液体部分经由管线2而从分离器D的沉降皿排出，并被供应至热交换器E1。通过其自己在热交换器E1内被过冷却的该液体部分，经由管线3而从热交换器E1排出，并在减压阀4内被减压。在热交换器E1内的气化(蒸发)一旦完成，该混合制冷剂支流(part stream)经由已提到过的管线5被供应至压缩机V1的第一压缩级。
气体部分经由管线6而从分离器D的顶部排出，并在压缩机V1的第二压缩级内被压缩至预期的最终压力。压缩的混合制冷剂流通过热交换器E3’中的环境空气或其他适合媒质被部分冷凝，并且经由管线7被供应至第二分离器D’。
汇聚在第二分离器D’的沉降皿内的液体部分经由管线8被进给回第一分离器D，在该管线8内设置了减压阀9。在分离器D’的顶部所得到的低沸点气体部分经由管线10被供应至热交换器E1，并在其中被冷却；该低沸点气体部分穿过热交换器E1后，经由管线11被供应至减压阀12。在经由所提到的管线5被供应至压缩机V1的第一压缩级前，混合制冷剂的支流在减压阀12被减压并且接着被再供应至热交换器E1，并在其中气化。
在根据本发明方法的一个改型中，建议富含碳氢化合物的气流的预冷却发生在螺旋形热交换器E1内。
根据其自身结构，螺旋形热交换器可以在其壳体内仅仅具有一个流道，但可选地在其管道内具有多个流道。因而可简单地在壳体内实现制冷剂(混合)的所有支流在正常压力下被气化。当使用螺旋形热交换器时，制冷剂(混合)的各支流在不同压力下的气化需要单独的装置。另外，螺旋形热交换器的管线比复杂板式热交换器结构的管线构造得更简单。
第二混合制冷剂循环中的用于把将要被液化的天然气气流液化和过冷却的压缩混合制冷剂首先经由管线20被进给至后冷却器E4，并且接着经由管线21被进给至热交换器E1并在此被冷凝。液化的混合制冷剂流接着经由管线22被供应至热交换器E2并在此被进一步过冷却；在穿过热交换器E2后，其在可选的减压涡轮T2内被减压；并且接着经由管线23其被供应至减压阀24并在此被减压。在热交换器E2内气化后，第二部分制冷剂流接着经由管线25被供应至再循环压缩机V2的引入级。
热交换器E2可以是螺旋形热交换器或板式热交换器的形式。如果富含碳氢化合物的气流的液化和过冷却在板式热交换器内发生，第二混合制冷剂循环中的混合制冷剂—根据本发明方法的有利的实施方式，可以以升流或降流的方式被气化。
根据本发明，现在，将要被液化的天然气气流的冷却、液化和过冷却通过两个混合制冷剂循环而发生；用于预冷却的混合制冷剂循环被分离为低沸点气体部分和高沸点液体部分；并且两个部分以不同的压力被供应至预冷却部。
已经发现，在同单向流液化方法对比后，根据本发明方法的能量消耗可减少10到20％。根据本发明的方法因而特别适合在1到3mtpa范围内的生产能力。
在双向流LNG装置内，回路压缩机通常由气轮机驱动。这些气轮机依次由电或气流驱动起动器使之投入运行。因为这些起动器必须具有相当大的功率—气轮机功率的20到40％，它们可被用作所谓的助动器(helper)，以在正常操作期间支持气轮机。市场上可买到的相对较大的气轮机仅仅具有离散的功率级以及相对大的功率跃变。气轮机的起动器或助动器的功率受到限制，以避免同步化问题。
由于大量技术上的因素，如将要被液化的富含碳氢化合物的气流的成分和压力、环境温度等等，并且由于可能需要将重质碳氢化合物分离，因此无法获得在两个混合制冷剂循环的压缩机驱动器之间的最适宜的功率分配、或者仅仅偶尔得到。常见地，第一或预冷却循环需要总能量的40到55％。另外，预冷却循环的功率需求经常是小于第二或液化循环的功率需求。
这种不对称可通过使用不同的助动器来均衡。例如，如果第一和第二混合制冷剂循环之间的功率分配是45％比55％，并且两个混合制冷剂循环的每一个循环分别具有一个功率为35MW的涡轮和一个功率为10MW的助动器，则第一制冷剂循环的助动器将以2MW的功率操作，而不是以可能的10MW的功率操作。在正常液化操作期间，将助动器作为投资的主要部分因而是没有利用价值的。
考虑到前面提到的与气轮机功率有关的起动器或助动器功率的限制，明显地，现所得到的两个助动器的完全利用导致了生产能力的最大化。参考以下实施例，将对此进行阐明。
如果获得第一和第二混合制冷剂循环之间50％比50％的功率分配—假定对于两个制冷剂循环具有同样的气轮机和起动器/助动器，则它们的这些装备和投资可被完全利用。返回到以上所指的实施例，第二制冷剂循环的起动器/助动器现在能以10MW的功率被操作。在与前面所提及的初始状态作对比后，根据本发明的方法的可用装机功率从82MW增加到了90MW。通过指定的驱动模式，生产输出因而可增加大约10％。
再循环压缩机V2—像再循环压缩机V1一样由气轮机G2所驱动，再循环压缩机V2是一个冷进气(cold-intake)压缩机并且优选地具有至少10∶1的压力比(压缩比)；起动器/助动器(未在附图中示出)与气轮机G1和G2连接。
部分压缩的混合制冷剂流经由管线26从再循环压缩机V2的中间级排出，其在冷却器E5经受到了后冷却并接着经由管线29至少部分地供应至热交换器E1，并且通过第一制冷剂循环在热交换器E1内被中间冷却。中间冷却后的、部分压缩的混合制冷剂流接着经由管线30再次被供应至压缩机V2的合适的中间压力级，并且被压缩至预期的最终压力。
依靠设有用于比例分配的阀28的管线27，可以调整经由管线29供应至热交换器E1的部分压缩混合制冷剂流的量。由于压缩机V2的高压部分的压缩功率与管线30内中间冷却的制冷剂流的低入口温度成比例减少，在以第一制冷剂循环为代价的情况下，使用第一制冷剂循环来实现第二制冷剂循环的中间冷却减少了第二制冷剂循环上的负载。各压缩机的输出是可变化的，直到在两个压缩机V1和V2之间和与它们相连的起动器/助动器之间实现输出均衡化。
以上所说明的中间冷却的最佳选择是由所选的用于第二制冷剂循环中的混合制冷剂的露点以及所选的混合制冷剂排出中间压力来决定的。理想地，依靠第一制冷剂循环，第二制冷剂循环中的一部分量的混合制冷剂被冷却直到两个循环的驱动器V1和V2被均衡化。
因为第一混合制冷剂循环现在被用于第二制冷剂循环的中间冷却，各相同气轮机和起动器/助动器的装机功率可被完全利用。
根据本发明方法的另一个实施例(未示出)仅仅在以下情况下使用，将要被液化的富含碳氢化合物的气流的预冷却之后才进行高沸点碳氢化合物的分离；其特征在于，第二混合制冷剂循环中的混合制冷剂流的支流被供应至分离单元H而实现冷却目的，并且接着以高于第二制冷剂循环中的剩余混合制冷剂流的压力被气化。因而，供应至分离单元H的混合制冷剂气体在气化后以合适的中间压力被供应至第二压缩机V2。
根据本发明用来实现富含碳氢化合物的气流的液化方法的缺点是，其需要比单向流液化方法更高的投资，并且，另外需要更加复杂和昂贵的控制技术。

Claims (4)

1.富含碳氢化合物的气流、特别是天然气气流的液化方法，富含碳氢化合物的气流的液化通过包括两个混合制冷剂循环的混合制冷剂级联循环而发生，第一混合制冷剂循环用于实现预冷却，第二混合制冷剂循环用于实现将被液化的富含碳氢化合物的气流的液化和过冷却；其特征在于，第一混合制冷剂循环(1至12)被分离为低沸点气体部分(10)和高沸点液体部分(2)，并且这两部分(2，10)以不同的压力被供应至预冷却部(E1)。
2.根据权利要求1所述方法，其特征在于，富含碳氢化合物的气流(a)的预冷却发生在螺旋形热交换器(E1)内。
3.根据权利要求1或2任一所述方法，其特征在于，每一个混合制冷剂循环包括由至少一个气轮机驱动的至少一个单级或多级压缩机，用来在正常操作期间支持气轮机的起动器与气轮机连接；第二混合制冷剂循环(20至25)包括具有至少10∶1的压力比的冷进气压缩机(V2)，第一混合制冷剂循环(1至12)至少部分地被用来实现第二混合制冷剂循环(20至25)中的部分压缩混合制冷剂流(26至29)的至少一个支流的中间冷却(E1)。
4.根据前面任一所述权利要求的方法，其特征在于，在将要被液化的富含碳氢化合物的气流被预冷却之后，高沸点碳氢化合物在分离单元内被分离出来；第二混合制冷剂循环(20至30)的一个支流的混合制冷剂流被供应至分离单元(H)以实现冷却目的，并接着以高于第二制冷剂循环(20至30)的剩余混合制冷剂流的压力被气化。
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CN102748918A (zh) * 2012-07-03 2012-10-24 中国海洋石油总公司 双级混合冷剂循环天然气液化系统
CN105473967A (zh) * 2013-03-15 2016-04-06 查特能源化工公司 混合制冷剂系统和方法
CN107869881A (zh) * 2016-09-27 2018-04-03 气体产品与化学公司 混合制冷剂冷却过程和系统

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CN102748918A (zh) * 2012-07-03 2012-10-24 中国海洋石油总公司 双级混合冷剂循环天然气液化系统
CN105473967A (zh) * 2013-03-15 2016-04-06 查特能源化工公司 混合制冷剂系统和方法
CN105473967B (zh) * 2013-03-15 2018-06-26 查特能源化工公司 混合制冷剂系统和方法
CN107869881A (zh) * 2016-09-27 2018-04-03 气体产品与化学公司 混合制冷剂冷却过程和系统
CN107869881B (zh) * 2016-09-27 2020-07-31 气体产品与化学公司 混合制冷剂冷却过程和系统

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