CN1042407A - 液化天然气蒸发气的再液化 - Google Patents

液化天然气蒸发气的再液化 Download PDF

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CN1042407A
CN1042407A CN89108306A CN89108306A CN1042407A CN 1042407 A CN1042407 A CN 1042407A CN 89108306 A CN89108306 A CN 89108306A CN 89108306 A CN89108306 A CN 89108306A CN 1042407 A CN1042407 A CN 1042407A
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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）蒸发气的方法。
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贮槽蒸发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蒸发气作辅助能源了。
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蒸发气。
对回收从贮槽中蒸发的含氮天然气蒸发气已做了一些工作。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%氮的蒸发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蒸发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蒸发气再液化的一种改进方法。在这种再液化蒸发气的方法中，闭合制冷设备包括如下步骤：
在具有初级和末级的多级压缩机设备中，压缩作为操作液体的氮使其成为一种压缩过的操作液体;将压缩过的操作液体分成第一和第二液流;等焓膨胀第一液流以产生一种冷却的第一液流，然后靠蒸发气来加热并靠再循环的压缩操作液体来加热;等熵膨胀第二液流，形成一种冷却的膨胀液流，然后靠蒸发气来加热并靠操作液体加热;最后，将所得加热过的等焓膨胀液流和等熵膨胀液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蒸发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，上述第一液流实现了等焓膨胀。
（b）如产生部份蒸气，则从液体中将其分离掉;
（c）靠蒸发气和再循环的压缩操作液体来加热蒸气;
（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）靠蒸发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液流;
（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蒸发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是用于回收蒸发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蒸发气，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操作液，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。经压缩的氮液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蒸发气。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分离。分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，然后在蒸发气压缩机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蒸发气所需的制冷作用是通过以氮作工作液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500～1000磅/英寸2。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，第一液流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-185°F～-85°F。经冷却的第一气流通过管路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25～125磅/英寸2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，靠蒸发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液流进行加热。液体通过管路15从分离器109抽出，然后在泵111中加压到约150～250磅/英寸2，再通过管路16送到热交换器110。在热交换器110中，蒸发气靠加压的液体制冷剂冷凝并冷却到其最低温度例如-290°F～-300°F。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，此外并能使再循环气流以较高的压力返回。
其余的制冷作用由第二液流30的等熵膨胀提供。第二液流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-75～-150°F，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25～125磅/英寸2，通常这与第一液流等焓膨胀的压力相同，然而它也可以是等焓膨胀液流和泵压液流压力的中间值。管路33将等熵膨胀液流输送到热交换器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，用于蒸发气制冷的最冷水平是通过工作液体等焓膨胀提供的，这不同于以等熵膨胀操作液作为制冷最冷水平的设备。
蒸发气的液化是以下述方式实现的：蒸发气通过管路1从贮存容器中取出并在蒸发气压缩机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蒸发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蒸发气的0～10%（体积），表1列出了气液流的性质和速度，速度按磅克分子/小时计，液流编号与图1中含氮0%的蒸发气所示的相同。
表2列出相应于图1所示编号气液流的现场性质，即含氮约10%（体积）的蒸发气的性质。
表3列出相当于美国专利3，874，185所述现有技术方法的气液流性质，其蒸发气的含氮量为0%。
表4列出美国专利3，874，185所述现有技术方法供液化的气液流性质，蒸发气含氮为10%。
表1
图1-Pumped JT-0%N2
气液流 N2CH4温度 压力
编号 磅克分子/小时 摩尔/小时 °F 磅/英寸2相态
1    -    292    -138    14.9    气态
2    -    292    -98    20    ″″
3    -    292    -254    18    ″″
4    -    292    -275    17    液态
5    -    292    -275    35    ″″
10    762    -    95    800    气态
11    762    -    -98    796    ″″
13    762    -    -254    788    ″″
14    762    -    -248    315    液态
15    581    -    -283    96    ″″
16    581    -    -279    240    ″″
18    581    -    -258    238    气态
19    581    -    -128    234    ″″
20    581    -    89    232    ″″
22    180    -    -283    96    ″″
23    180    -    -128    92    ″″
24    180    -    89    90    ″″
30    1720    -    95    800    ″″
31    1720    -    -98    796    ″″
32    1720    -    -112    794    ″″
33    1720    -    -261    96    ″″
36    1720    -    -128    92    ″″
37    1720    -    89    90    ″″
38    1901    -    89    90    ″″
表2
图1-Pumped JT-10%N2
气液流 N2CH4温度 压力
编号 磅克分子/小时 摩尔/小时 °F 磅/英寸2相态
1    32    289    -202    15.5    气态
2    32    289    -175    20    ″″
3    32    289    -256    18    ″″
4    32    289    -296    16    液态
10    739    -    99    800    气态
11    739    -    -122    796    ″″
13    739    -    -246    788    液态
14    739    -    -300    45    气态
15    492    -    -304    36    液态
16    492    -    -301    164    ″″
17    492    -    -260    162    气态
18    739    -    -304    43    ″″
19    492    -    94    156    ″″
20    492    -    98    156    ″″
26    1736    -    94    88    ″″
30    1736    -    99    800    ″″
32    1736    -    -122    792    ″″
33    1736    -    -267    96    ″″
36    1736    -    -159    92    ″″
37    1736    -    95    90    ″″
表3
现有技术-图2-美国专利3，874，185-0%N2
气液流 N2CH4温度 压力 相态或
编号 磅克分子/小时 摩尔/小时 °F 磅/英寸2露点（℃）
1    -    292    -138    14.9    气态
2    -    292    -38    30    ″″
3    -    292    -243    28    气+液
4    -    292    -276    27    液态
45    2368    -    95    653    气态
46    2368    -    -150    647    ″″
47    2368    -    -278    91.1    ″″
48    2368    -    -245    88.1    ″″
60    2368    -    90    85    ″″
52    415    -    95    653    ″″
54    415    -    -243    641    液态
55    415    -    -247    348    ″″
56    415    -    -126    343    气态
58    415    -    90    337    ″″
表4
现有技术-图2-美国专利3，874，185-10%N2
气液流 N2CH4温度 压力
编号 磅克分子/小时 摩尔/小时 °F 磅/英寸2相态
1    32    289    -202    15.5    气态
2    32    289    -125    30    ″″
3    32    289    -260    28    气+液
4    32    289    -296    27    液态
5    32    289    -295    60    ″″
45    2056    -    99    653    气态
46    2056    -    -164    480    ″″
47    2056    -    298    48    ″″
48    2056    -    -263    45    ″″
60    2056    -    94    42    ″″
52    391    -    99    653    ″″
54    391    -    -260    641    ″″
55    391    -    -263    202    气+液
56    391    -    -150    197    气态
58    391    -    94    191    ″″
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    蒸发气    热交换器    功率
N2% UA（BTU/小时°F） （马力）
表1    0    792，244    2，724
表2    10    713，445    3，050
表3    0    797，110    2，801
表4    10    702，094    3，550
从这些结果可以看到，在蒸发气含氮为0～10%范围内，Pumped    JT设备（表1和2）优于图2的现有技术的设备。

Claims (7)

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蒸发气的方法，该蒸发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设备包括下列步骤：
在有初级和末级的多级压缩机设备中，压缩作为工作液体的氮使其成为压缩的工作液体；
将所述压缩的工作液体分成第一和第二液流；
等焓膨胀所述第一液流以产生冷却的第一液流，然后靠再循环的压缩工作液体和蒸发气来加热；
等熵膨胀第二液流以产生冷却的膨胀液流，然后在被输送回压缩机设备之前靠蒸发气和工作液体加热；
再液化含氮约为0～10%(体积)的蒸发气的改进之处包括：
(a)在至少生成一部份液体的条件下，将所述第一液流进行等焓膨胀。
(b)产生部份蒸气时，从液体中将其分离掉；
(c)如产生蒸气，则靠蒸发气和再循环的压缩工作液体来加热蒸气；
(d)用泵将(a)步产生的液体加压；
(e)靠蒸发气首先加热经加压的液体，然后平行地加热上述等熵膨胀的第二液流。
2、如权利要求1所述的方法，其特征在于，氮工作液体被压缩到约500～1000磅/英寸2。
3、如权利要求2所述的方法，其特征在于，第一液流进行等焓膨胀之前被冷却到约-185～85°F。
4、如权利要求3所述的方法，其特征在于，第一液流在等焓膨胀中膨胀到压力为25～125磅/英寸2。
5、如权利要求4所述的方法，其特征在于，第二液流进行等熵膨胀前被冷却到约-75～-150°F。
6、如权利要求5所述的方法，其特征在于，第二液流膨胀到压力为约25～125磅/英寸2。
7、如权利要求6所述的方法，其特征在于，等焓膨胀后的液体压力提高到约125～275磅/英寸2并被送回到多级压缩机设备的初级和末级之间的一级。
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EP0367156A2 (en) 1990-05-09
US4843829A (en) 1989-07-04
KR930008299B1 (ko) 1993-08-27
EP0367156A3 (en) 1990-07-04
KR900008010A (ko) 1990-06-02
JPH02157583A (ja) 1990-06-18
CN1018578B (zh) 1992-10-07

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