CN102410702A - 天然气的液化 - Google Patents

天然气的液化 Download PDF

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CN102410702A
CN102410702A CN2011102940978A CN201110294097A CN102410702A CN 102410702 A CN102410702 A CN 102410702A CN 2011102940978 A CN2011102940978 A CN 2011102940978A CN 201110294097 A CN201110294097 A CN 201110294097A CN 102410702 A CN102410702 A CN 102410702A
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H·鲍尔
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Abstract

本发明描述了将富烃原料馏分优选天然气与氮制冷回路相对地进行液化的方法，其中将原料馏分与待加热的气态氮相对地进行冷却，及将原料馏分与待蒸发的液态氮相对地进行液化。根据本发明，在至少三级的热交换过程(E1a-E1c)中将原料馏分冷却和液化；其中在热交换过程的第一区段(E1a)中将原料馏分(1)与过热的气态氮(9)相对地进行冷却，直至实现基本上完全分离出(D2)较重的成分(2′)；在热交换过程的第二区段(E1b)中将去除了较重成分的原料馏分(2)与待过热的气态氮(9)相对地进行部分液化；及在热交换过程的第三区段(E1c)中将原料馏分(2)与有待部分蒸发的氮(8)相对地进行液化。

Description

天然气的液化
技术领域
本发明涉及使富烃原料馏分尤其是天然气与氮制冷回路相对地液化的方法，其中将原料馏分与待加热的气态氮相对地进行冷却，及将原料馏分与待蒸发的液态氮相对地进行液化。 
背景技术
富烃气体尤其是天然气的液化在商业上在每天10至30,000吨LNG(日吨产量)的产量范围内进行。对于中型产能的设备即具有300至3,000吨LNG的日吨产量的液化过程和大型产能的设备即具有3,000至30,000吨LNG的日吨产量的液化过程，本领域技术人员努力通过高效率最优化运行成本。与此不同，对于更小型的设备即具有10至300吨LNG的日吨产量的液化过程，重视低的投资成本。对于此类设备，其中例如将氮或氮-烃混合物用作工作介质的自身制冷装置的投资成本比例相当大。因此，任选地省略掉在液化装置中的制冷，并引入合适的制冷剂。在此情况下通常使用液态氮，并在将其用作制冷剂之后以气态形式排放至大气。若位于附近的空气分离设备能够以低廉成本提供未使用的产品量的液态氮，则这一构思对于小型液化设备而言很有商业价值。 
出于成本原因，对于小型液氮冷却的设备，通常使用焊接的铝片式热交换器。但是该装置对强烈的热负荷很敏感，强烈的热负荷是其例如通过制冷剂的过量供应和/或在热与冷的工艺流之间大的温差而引起的。所产生的机械应力会造成该装置的损坏。 
此外还应当注意的是，在液化过程中不允许低于原料馏分的凝结温度。甲烷的凝结点为-182℃，明显高于氮的常压沸点-196℃。设备冻结总是会引起非期望的运行故障，而且会额外造成永久性损坏。 
第5,390,499号美国专利公开了一种使富烃原料馏分液化的方法。该方法尤其适合于如前所述的小型产能设备。在该第5,390,499号美国专利所述的液化方法中，待液化的气体在两个分离的热交换器中与氮相对地进行冷却及液化。在此，低沸点的液态氮在第二热交换器中完全蒸发，直至加热到一个温度，在该温度下可以利用分离塔从待液化的气体以液态形式排出较重的原料气成分。但是在第5,390,499号美国专利中所述的工艺过程中，使氮完全蒸发的位点可以取决于负荷剧烈波动。这会导致非期望的工艺条件，而产生上述缺点。 
发明内容
本发明的目的在于，阐述使富烃原料馏分液化的方法，其避免了上述缺点，并且尤其是提供不易发生运行故障和损坏的方法。 
为了实现该目的，建议使富烃原料馏分液化的方法，其特征在于， 
-在至少三级的热交换过程中将原料馏分冷却及液化， 
-其中在该热交换过程的第一区段中将原料馏分与过热的气态氮相对地进行冷却，直至实现基本上完全分离出较重的成分， 
-在该热交换过程的第二区段中将去除了较重成分的原料馏分与待过热的气态氮相对地进行部分液化，及 
-在该热交换过程的第三区段中将原料馏分与有待部分蒸发的氮相对地进行液化。 
术语“重的成分”是指乙烷以上的烃类。 
根据本发明的使富烃原料馏分液化的方法的其他有利的实施方案的特征在于， 
-在一个或多个热交换器中实施三级热交换过程， 
-将去除了较重成分的原料馏分的凝结压力调节到1至15巴、优选1至8巴的数值，及 
-将待过热的气态氮的沸腾压力调节到5至30巴、优选10至20巴的数值。 
以下将根据附图所示的实施例，详细解释根据本发明的富烃原料馏分液化方法以及该方法的其他有利的实施方案。
附图说明
图1所示为根据本发明的实施方案。 
具体实施方式
将待液化的富烃原料馏分经过管路1送至热交换器E1。该热交换器分为a至c三个区段或阶段。在这些区段或阶段之间的界限由两条虚线显示。在热交换器E1的最热的区段a中，将富烃原料馏分与经过管路9送至热交换器E1的过热的气态氮相对地进行冷却，直至可以在设置在热交换器E1下游的分离塔D2中将重的成分从原料馏分中分离出。为此将冷却的原料馏分从热交换器E1经过管路1′送至分离塔D2。从分离塔的塔底经过其中设置有阀门V1的管路2′排出非期望的重的液态成分，并从该过程排出。 
可以使用精馏塔代替附图中所示的分离塔D2，精馏塔更加精确地从原料馏分中分离出重的成分或更高级的烃类。 
在分离塔D2的塔顶上经过管路2排出去除了重的成分的原料馏分，并送至热交换器E1的第二区段b。在其中将去除了重的成分的原料馏分与待过热的气态氮9相对地进行部分液化。随后在热交换器E1的第三阶段c中将原料馏分与经过管路8送至热交换器E1的有待部分蒸发的氮相对地进行完全液化。 
液化的原料馏分在经过热交换器E1之后，经过其中设置有调节阀V3的管路3送至储存容器D4。由此可以将液化的产品(LNG)经过管路4排出。调节阀V3用于将液化的原料馏分减压到至少近似地对应于大气压的产品排出压力。 
若氮在热交换器E1的第三区段c中在大于15巴的压力下进行蒸发，则其沸腾温度不再足够低以使液化的原料馏分过冷至可以防止在调节阀V3中减压之后发生气体泄出的程度。在此类情况下，优选将在储存容器D4中产生的挥发气(Boil-off-Gas)经过管路5排出，在压缩机C3中进行压缩，并在其液化之前再次送至去除了重的成分的原料馏分2，并在热交换器E1中再次液化。尤其是在大气压的平底储罐D4中值得一提地临时储存LNG产品时选择该方法过程，因为由此还处理所产生的挥发气。 
将提供冷量所需的氮经过管路6送至液化过程。优选设置缓冲容器D3，其用于平衡待液化的原料馏分和/或氮制冷剂的量的波动。利用泵P1将液态氮以所需的量经过管路7送至分离塔D1。从分离塔D1的塔底排出沸腾的氮，并经过管路8使其通过热交换器E1的最冷的区段c。随后将在此部分蒸发的氮经过管路8′重新送至分离塔D1。 
若实施尚待描述的再液化过程，则通过氮的再液化所产生的冷量可以至少暂时地超过天然气液化所需的冷量。可以将由此产生的液态氮的过量供应经过管路8″和阀门V6排出到缓冲容器D3中。 
在分离塔D1的塔顶经过管路9排出气态氮，并送至热交换器E1的中间区段b。在相对于待冷却和有待部分液化的原料馏分2的逆流中，使气态氮通过热交换器E1的第二和第一区段，并在此进行加热以及过热。随后将过热的氮经过管路区段10和11从该过程排出。 
利用调节阀V4可以调节待过热的气态氮9的沸腾压力。优选将该沸腾压力调节到5至30巴、更优选10至20巴的数值。 
以类似的方式，利用调节阀V2可以调节去除了较重成分的原料馏分2的凝结压力。优选将该凝结压力调节到1至15巴、更优选1至8巴的数值。 
所以利用调节阀V2和/或V4可以控制热交换器E1的第三区段c中的温度分布。利用调节阀V2设定在调节阀V2和V3之间的区段中原料 馏分的凝结压力，而利用调节阀V4则调节在分离塔D1和热交换器E1的第三区段c中氮的沸腾压力。由于之前所述将热交换过程划分成第二和第三区段，并利用在分离塔D1中的相分离，现在可以精确设定在热交换器E1的哪个区段中使氮(部分)蒸发或过热。 
通过将热交换过程E1划分成三个区段a至c，可以可靠地防止在热交换器E1中在液态和气态制冷剂之间的相界迁移，并由此在热交换器E1中产生非期望的热应力和机械应力。 
若根据不等式pRG(巴)≥0.3pN2(巴)-1选择氮的沸腾压力(pN2)和原料气的凝结压力(pRG)，则可靠地避免由于不允许的大的温差引起热交换器E1的热过载。 
通过将在热交换器E1的第三区段c中的和分离塔D1的液态氮的沸腾压力限制到至少5巴，相应的沸腾温度为-179℃，可以可靠地防止在热交换器E1中出现低于甲烷的凝结温度的温度。由此防止由于形成固体而出现运行问题和任选存在的损坏。 
作为经过管路11进行导出的其他选择，经过管路10从热交换器E1排出的过热的氮可以至少部分地再液化。为此将氮经过管路区段12和13送至压缩装置，其在附图中由两级压缩机单元C1/C2表示，其中每个压缩机单元下游设置有热交换器E3或E4，随后经过管路14送至热交换器E2。在其中使氮再液化，然后经过管路15送至分离塔D1。通过调节阀V5调节压缩机C2的压力。为了在热交换器E2中提供冷量，经过管路16排出压缩的氮流的支流，优选多级减压，其由气体膨胀机X1和X2表示，随后经过管路17在相对于待液化的氮流的逆流中引导通过热交换器E2。压缩机C1和C2的轴优选与气体膨胀机X2和X1的轴相连。 
若实施之前所述的再液化过程，则优选将对于在热交换器E1的热端处的流1和10之间约3℃的小的正温差所需的量的气态氮经过管路9送至热交换器E1。将过量的低温气态氮经过管路9′按比例用于在热交换器E2中进行的再液化。 
液化过程原则上可以利用“引入的”氮进行，在此情况下过热的氮从热交换器E1经过管路区段10和11排出，利用再液化的氮进行或者通过这两种运行方式的任意组合进行。 

Claims (4)

1.将富烃原料馏分优选天然气与氮制冷回路相对地进行液化的方法，其中将原料馏分与待加热的气态氮相对地进行冷却，及将原料馏分与待蒸发的液态氮相对地进行液化，其特征在于，
-在至少三级的热交换过程(E1a-E1c)中将原料馏分冷却和液化，
-其中在热交换过程的第一区段(E1a)中将原料馏分(1)与过热的气态氮(9)相对地进行冷却，直至实现基本上完全分离出(D2)较重的成分(2′)，
-在热交换过程的第二区段(E1b)中将去除了较重成分的原料馏分(2)与待过热的气态氮(9)相对地进行部分液化，及
-在热交换过程的第三区段(E1c)中将原料馏分(2)与有待部分蒸发的氮(8)相对地进行液化。
2.根据权利要求1的方法，其特征在于，在一个或多个热交换器中实现三级热交换过程(E1a-E1c)。
3.根据权利要求1或2的方法，其特征在于，将去除了较重成分的原料馏分(2)的凝结压力调节(V2)到1至15巴、优选1至8巴的数值。
4.根据权利要求1至3之一的方法，其特征在于，将待过热的气态氮(9)的沸腾压力调节(V4)到5至30巴、优选10至20巴的数值。
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