CN1018578B - 液化天然气逸气的再液化 - Google Patents

液化天然气逸气的再液化

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CN1018578B
CN1018578B CN89108306A CN89108306A CN1018578B CN 1018578 B CN1018578 B CN 1018578B CN 89108306 A CN89108306 A CN 89108306A CN 89108306 A CN89108306 A CN 89108306A CN 1018578 B CN1018578 B CN 1018578B
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CN1042407A (zh
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韦恩·戈登·斯图伯
肯尼思·威廉·科瓦克
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Air Products and Chemicals Inc
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Abstract

本发明涉及一种用于再液化由装在贮存容器中的液化天然气蒸发而产生的含氮达10%的蒸发气的改进方法。在该方法中，采用了一个闭合氮制冷循环，其中氮在产生液体和蒸气的条件下进行等焓膨胀，将液体用泵加压并靠初步冷却的蒸发气流加热。蒸发的LNG气流通过与等熵膨胀的制冷气流间接热交换达到初步冷却。

Description

本发明涉及一种从贮存容器中回收液化天然气（LNG）逸气的方法。
在装载液化天然气（LNG）的海上油船及陆地的贮槽中，由于通过LNG贮槽周围的绝热体热渗透造成一部份液化天然气蒸发而损失掉。一般损失量每天约为0.1到0.25%。此外，热量渗透进入陆地和海上的LNG贮存容器造成某些液态天然气蒸发，因而增加了容器内的压力。
船上的LNG贮槽逸气通常被用作为一种辅助燃料来驱动船上的锅炉和发动机。可是目前LNG船体设计已装上柴油机而不用蒸气驱动的发动机，因此就不需要使用LNG逸气作辅助能源了。
最近颁布的禁止在大城市附近泄放或燃烧处理含烃气体的法规，以及进一步节省能源成本的要求，都促使把再液化器并入新油船设计中以回收LNG逸气。
对回收从贮槽中蒸发的含氮天然气逸气已做了一些工作。通常这些装置采用一种闭合制冷装置，其中循环气经过压缩、冷却和膨胀而起到制冷作用，然后再返回压缩机。代表性的专利如下：
美国专利3，874，185公开了一种利用闭合氮制冷循环的再液化方法，其中冷凝LNG的最低级或最冷级制冷作用由一种等熵膨胀 气液流提供，而其余的制冷作用由剩余的第二部份制冷剂的等焓膨胀提供。在一个实施例中，等焓膨胀过的剩余部分气液流经相分离使液体和气体分开。需要低制冷时，一部分液体贮存着，而需要较高制冷时，所贮存的一部分液体则再循环进入制冷设备。
本发明提供了一种用于使含0-约10%氮的逸气再液化的灵活而高效的方法。现有技术的方法一般无法使含氮量在如此宽范围内的逸气进行有效的再液化。它们只适用于很窄浓度范围内的操作。如果杂质浓度偏离设计规范，那么再液化器的效率就降低了。本发明的实施例则排除了这种不足之处。
本发明是采用闭合氮制冷循环的方法，将贮槽中的液化天然气蒸发所产生的LNG逸气再液化的一种改进方法。在这种再液化逸气的方法中，闭合制冷方法包括如下步骤：
在具有初级和末级的多级压缩机设备中，压缩作为工作流体的氮使其成为一种压缩过的工作流体：将压缩过的工作流体分成第一和第二物流;等焓膨胀第一物流以产生一种冷却的第一物流，然后靠逸气来加热并靠再循环的压缩工作流体来加热;等熵膨胀第二物流，形成一种冷却的膨胀物流，然后靠逸气来加热并靠工作流体加热;最后，将所得加热过的等焓膨胀物流和等熵膨胀物流送回到多级压缩机设备中。
在闭合制冷方法中，将含约0-10%（体积）氮的LNG逸气再液化的改进之处包括：
（a）在至少产生一部分液体的条件下，上述第一物流实现了等焓膨胀。
（b）如产生部份蒸气，则从液体中将其分离掉;
（c）靠逸气和再循环的压缩工作流体来加热蒸气;
（d）将至少一部份在（a）步骤形成的液体加压至多级压缩机设备的初级和末级之间的压力;
（e）靠逸气首先加热所得的已加压的液体，然后平行地加热上述等熵膨胀的第二物流;
（f）将所得加热后的加压液体送回到多级压缩机设备中的一级。
本发明具有若干优点：
（a）能使制冷剂循环气的加热曲线和LNG逸气的冷却曲线更相吻合，因此减少了液化所需的能量;
（b）能得到较高的效率，有助于降低液化所需的热交换器表面积。
图1是说明称为Pumped    JT方法的闭合方法的流程图。
图2是用于回收逸气的现有技术闭合方法的流程图。
本方法用于再液化从装在贮存容器中的液化天然气蒸发所产生的逸气，它的改进之处是通过改进闭合制冷设备而达到的。通常，闭合制冷设备以氮作制冷剂或工作流体，在一般方法中，氮通过有初级和末级并通常配备后冷却器的一系列多级压缩机进行压缩而达到预定的压力。经压缩的氮流分成一部份进行等焓膨胀而另部份进行等熵膨胀。典型地，由等熵膨胀所得的功被用于驱动末级压缩。通过这种等焓和等熵膨胀发生了制冷作用。这种制冷作用用来再液化逸气。目的是要使冷却曲线与加热曲线相吻合，避免这两曲线之间严重偏离。曲线偏离是制冷值损失的证据。
为有利于了解本发明，参考图1。图1所示的称为Pumped    JT方法的实施例中，要再液化的天然气（甲烷）通过管路1从贮槽（图 上没有表示）取得，然后在逸气压缩机100中压缩达到一定压力以满足再液化加工时的要求。
再液化LNG逸气所需的制冷作用是通过以氮作工作流体或循环气的闭合制冷设备而提供的。在这种制冷设备中，氮通过有后冷却器102的一系列多级压缩机从常压压缩到一个足够的压力，如34-68大气压。热力效率由于在氮循环中使用较大的压力差而提高。
在再液化方法中，第一物流10在热交换器104中冷却，然后通过管路11再在热交换器106中冷却至温度约-120℃--65℃。经冷却的第一物流通过管路13取出，并在JT阀108中在足以生成液体的条件下膨胀，达到例如约1.7-8.5大气压的压力。等焓膨胀后的分离器109可以贮存液体以备其后流速或组份变化时应用，同时若膨胀时产生蒸气，则可从液体中将它分离掉。任何分离器109中的蒸气可通过管路22引出，靠逸气来加热并在其经管路23和24回到多级压缩机设备102以前以未进行等焓膨胀的第一物流进行加热。液体通过管路15从分离器109抽出，然后在泵111中加压到约10.2-17.0大气压，再通过管路16送到热交换器110。在热交换器110中，逸气靠加压的液体制冷剂冷凝并冷却到其最低温度例如-180℃--185℃。然后加压的液体经管路18、19和20通过热交换器106和104加热到蒸气状态而回到多级压缩机设备102的初级和末级之间的一级。应用压力可以使冷却曲线和加热曲线更相吻合，特别在比用其它方法氮含量更高时，此外并能使再循环物流以较高的压力返回。
其余的制冷作用由第二物流30的等熵膨胀提供。第二物流30在热交换器104再通过管路31在热交换器106中冷却到温度约为-60--100℃，然后通过管路32输送到膨胀器112中，然后等熵膨胀到压力 约为1.7-8.5大气压，通常这与第一物流等焓膨胀的压力相同，然而它也可以是等焓膨胀物流和泵压物流压力的中间值。管路33将等熵膨胀物流输送到热交换器106，然后通过管路36进入热交换器104，再经过管路37进入压缩机设备102。因此，用于逸气制冷的最冷水平是通过工作流体等焓膨胀提供的，这不同于以等熵膨胀工作流体作为制冷最冷水平的设备。
逸气的液化是以下述方式实现的：逸气通过管路1从贮存容器中取出并在逸气压缩机100中压缩，然后再通过管路2、3和4经热交换器106和110而液化。液化的LNG从热交换器110出口经管路4引出并在泵114中加压，然后经管路5输送到贮存容器中。
下述实例用来说明本发明的各种具体方案，但并非限制本发明的范围。
实例1
Pumped    JT法
LNG逸气回收体系按照如前所述图1的方法的流程进行。氮浓度变化范围约为逸气的0-10%（体积），表1列出了物流的性质和速度，速度按千克摩尔/小时计，物流编号与图1中含氮0%的逸气所示的相同。
表2列出相应于图1所示编号物流的现场性质，即含氮约10%（体积）的逸气的性质。
表3列出相当于美国专利3，874，185所述现有技术方法的物流性质，其逸气的含氮量为0%。
表4列出美国专利3，874，185所述现有技术方法供液化的物流性质，逸气含氮为10%。
表1
图1-Pumped JT-0%N2
物流 N2CH4温度 压力编号
编号    （千克摩尔    （摩尔/    （℃）    （大气压）    相态
/小时）    小时）
1    -    292    -94    1.01    气态
2    -    292    -72    1.36    ′′′′
3    -    292    -159    1.22    ′′′′
4    -    292    -171    1.16    液态
5    -    292    -171    2.38    ′′′′
10    346    -    35    54.4    气态
11    346    -    -72    54.1    ′′′′
13    346    -    -159    53.6    ′′′′
14    346    -    -156    21.4    液态
15    264    -    -175    6.53    ′′′′
16    264    -    -173    16.3    ′′′′
18    264    -    -161    16.2    气态
19    264    -    -89    15.9    ′′′′
20    264    -    32    15.8    ′′′′
22    82    -    -175    6.53    ′′′′
23    82    -    -89    6.26    ′′′′
24    82    -    32    6.12    ′′′′
30    780    -    35    54.4    ′′′′
31    780    -    -72    54.1    ′′′′
32    780    -    -80    54.0    ′′′′
33    780    -    -163    6.53    ′′′′
36    780    -    -89    6.26    ′′′′
37    780    -    32    6.12    ′′′′
38    862    -    32    6.12    ′′′′
表2
图1-Pumped JT-10%N2
物流 N2CH4温度 压力
编号    （千克摩尔    （摩尔/    （℃）    （大气压）    相态
/小时）    小时）
1    15    289    -130    1.05    气态
2    15    289    -115    1.36    ′′′′
3    15    289    -160    1.22    ′′′′
4    15    289    -182    1.09    液态
10    335    -    37    54.4    气态
11    335    -    -86    54.1    ′′′′
13    335    -    -154    53.6    液态
14    335    -    -184    3.06    气态
15    223    -    -187    2.45    液态
16    223    -    -185    11.2    ′′′′
17    223    -    -162    11.0    气态
18    335    -    -187    2.92    ′′′′
19    223    -    34    10.6    ′′′′
20    223    -    37    10.6    ′′′′
26    787    -    34    5.98    ′′′′
30    787    -    37    54.4    ′′′′
32    787    -    -86    53.9    ′′′′
33    787    -    -166    6.53    ′′′′
36    787    -    -106    6.26    ′′′′
37    787    -    35    6.12    ′′′′
表3
现有技术-图2-美国专利3，874，185-0%N2
物流 N2CH4温度 压力 相态或
编号    （千克摩尔    （摩尔/    （℃）    （大气压）    露点（℃）
/小时）    小时）
1    -    292    -94    1.01    气态
2    -    292    -39    2.04    ′′′′
3    -    292    -153    1.90    气+液
4    -    292    -171    1.84    液态
45    1074    -    35    44.4    气态
46    1074    -    -101    44.0    ′′′′
47    1074    -    -172    6.19    ′′′′
48    1074    -    -154    5.99    ′′′′
60    1074    -    32    5.78    ′′′′
52    188    -    35    44.4    ′′′′
54    188    -    -153    43.6    液态
55    188    -    -155    23.7    ′′′′
56    188    -    -88    23.3    气态
58    188    -    32    22.9    ′′′′
表4
现有技术-图2-美国专利3，874，185-10%N2
物流 N2CH4温度 压力
编号    （千克摩尔    （摩尔/    （℃）    （大气压）    相态
/小时）    小时）
1    15    289    -130    1.05    气态
2    15    289    -87    2.04    ′′′′
3    15    289    -162    1.90    气+液
4    15    289    -182    1.84    液态
5    15    289    -182    4.08    ′′′′
45    933    -    37    44.4    气态
46    933    -    -109    32.6    ′′′′
47    933    -    148    3.26    ′′′′
48    933    -    -164    3.06    ′′′′
60    933    -    34    2.60    ′′′′
52    177    -    37    44.4    ′′′′
54    177    -    -162    43.6    ′′′′
55    177    -    -164    13.7    气+液
56    177    -    -101    13.4    气态
58    177    -    34    13.0    ′′′′
经计算求出热交换器条件，以U乘A表示，其中U为热传递系数，A为前列表1-4中方法的热交换器表面积。还给出了所需的压缩机功率。这些数值列于表5中。
表5
方法    逸气    热交换器    功率
N2% UA（千卡/小时℃） （千瓦）
表1    0    110，914    2031
表2    10    99，882    2274
表3    0    111，595    2089
表4    10    98，293    2647
从这些结果可以看到，在逸气含氮为0-10%范围内，PumpedJT设备（表1和2）优于图2的现有技术的设备。

Claims (6)

1、一种用于液化由装在贮存容器中的液化天然气蒸发而产生的逸气的方法，该逸气在闭合的氮制冷设备中被冷却并液化，然后送回上述的贮存容器中，其中所述的闭合制冷方法包括下列步骤：
在有初级和末级的多级压缩机设备中，压缩作为工作流体的氮使其成为压缩的工作流体；
将所述压缩的工作流体分成第一和第二物流；
等焓膨胀所述第一物流以产生冷却的第一物流，然后靠再循环的压缩工作流体和逸气来加热；
等熵膨胀第二物流以产生冷却的膨胀物流，然后在被输送回压缩机设备之前靠逸气和工作流体加热；
再液化含氮约为0-10%(体积)的逸气的方法的特征在于：
(a)在至少生成一部份液体的条件下，将所述第一物流进行等焓膨胀；
(b)产生部份蒸气时，从液体中将其分离掉；
(c)如产生蒸气，则靠逸气和再循环的压缩工作流体来加热蒸气；
(d)用泵将(a)步产生的液体加压；
(e)靠逸气首先以热交换关系加热经加压的液体，然后以热交换关系加热上述等熵膨胀的第二物流。
2、如权利要求1所述的方法，其特征在于，氮工作流体被压缩到约34-68大气压。
3、如权利要求2所述的方法，其特征在于，第一物流进行等焓膨胀之前被冷却到约-120℃--65℃。
4、如权利要求3所述的方法，其特征在于，第一物流进行等焓膨胀中膨胀到压力为1.7-8.5大气压。
5、如权利要求4所述的方法，其特征在于，第二物流进行等熵膨胀前被冷却到约-60℃--100℃。
6、如权利要求5所述的方法，其特征在于，第二物流膨胀到压力为约1.7-8.5大气压。
CN89108306A 1988-11-03 1989-11-03 液化天然气逸气的再液化 Expired CN1018578B (zh)

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