CN1041440A - 使用低级、高级和吸收制冷循环进行天然气液化的方法 - Google Patents

使用低级、高级和吸收制冷循环进行天然气液化的方法 Download PDF

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CN1041440A
CN1041440A CN89107430A CN89107430A CN1041440A CN 1041440 A CN1041440 A CN 1041440A CN 89107430 A CN89107430 A CN 89107430A CN 89107430 A CN89107430 A CN 89107430A CN 1041440 A CN1041440 A CN 1041440A
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heat pump
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CN1013803B (zh
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查尔斯·里奥·牛顿
罗伯特·牛顿·戴维斯
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Abstract

本发明是一种有关天然气液化的改进方法。其液化方法中的制冷是由两条闭合制冷循环所提供的。初级或低级制冷循环使用一种混合的制冷剂作为热泵流体。第二级或高级制冷循环使用一种混合的(多组分)制冷剂作热泵流体。在该液化方法中，第二级或高级制冷循环冷却低级热泵流体。低级制冷循环冷却并液化天然气原料。方法的改进之处是采用了一条吸收制冷循环来预冷天然气原料、低级热泵流体、高级热泵流体和(如需要话)深度闪蒸再循环液，使吸收制冷循环运转的热量是由该方法中来自一个或几个压缩机的传动装置的废气所供给的。

Description

本发明涉及一种液化天然气的方法。具体讲，本发明涉及使用低级、高级和吸收热泵循环使天然气冷却和液化的一种液化方法。
众所周知，天然气等气体的液化已有众多方法，其中最适宜参考的方法如下：
美国专利4，545，795公开了一种使用两条闭合循环，多组分制冷剂进行液化天然气的方法和装置。该方法中低级制冷冷却和液化天然气，而高级制冷冷却并部分液化低级制冷剂。为使用较轻的制冷组分以完成最后的最低级制冷将高级制冷剂进行相分离，而为避免多级闪蒸分离而将分离的液相分开，然后被膨胀以达到制冷作用。其中较重组分被利用来提供低级制冷作用。
美国专利4，525，195公开了一种利用两条闭合循环、多组分制冷剂液化天然气的改进方法和装置。低级制冷冷却天然气，而高级制制冷冷却低级制冷剂，方法的改进之处包括了相分离压缩后的高级制冷剂和相对于附加压缩后的外部冷却液充分地液化了蒸气相气流。
美国专利3，812，046公开了一种天然气液化方法。该方法采用一条多组分冷却循环结合一条吸收制冷循环，该发明利用多组分循环中压缩机的驱动装置废气来实现吸收制制冷循环的加热过程。
美国专利3，763，658公开了一种液化原料气的方法和制冷体系。该方法中首先将原料气在一个密闭的阶式循环中与单组分制冷剂进行热交换，然后再将原料气在一个多段热交换器中与一种多组分制冷剂进行热交换，因而形成为第二级密闭的制冷循环。
其它的有关制冷循环或液化方法已公开在美国专利2，826，049、2，909，905、3，212，276、3，418，819、和3，611，739中。
本发明是一种有关天然气液化的改进方法。其中液化方法的制冷过程是由两条闭合的制冷循环所提供的。初级或低级制冷循环中以一种混合（多组分）的制冷剂作为热泵流体（heat    pump    fluid），第二级或高级制冷循环中以混合的制冷剂作热泵流体。在液化方法中，第二级或高级制冷循环冷却低级热泵流体并可任选作初步地冷却天然气原料。低级制冷循环冷却并液化冷后的天然气原料。随意地，至少一部分已液化的天然气可被闪蒸从而形成闪蒸液流，同时至少一部分这种闪蒸后的液流将再被压缩并再循环回到方法中作为深度闪蒸液流。本方法的改进之处是利用一条吸收制冷循环以预冷天然气原料、低级热泵流体、高级热泵流体及，随意地，深度闪蒸液流。使吸收制冷循环运转的热量可由方法中压缩机的传动装置废气供给。
图1是一张利用两条闭合制冷循环液化天然气方法的简化流程图。
图2是一张本发明所述方法的简化流程图，其中包括了吸收制冷循环。
图3是一张吸收制冷循环流程图，表示了该循环和图2方法之间的相互关系。
如上所述，本发明一种关于天然气液化的改进方法。其中液化方法的制冷过程是由两条闭合的制冷循环所提供的。初级或低级制冷循环以一种混合（多组分，如氮、甲烷、乙烷和丙烷的混合物）的制冷剂作为热泵流体，而第二级或高级制冷循环以一种混合的或一种单组分（如丙烷）的制冷剂作热泵流体。制冷循环可以是任何制冷循环，如阶式循环、多段热交换循环、多组分相分离循环等。
在该液化方法中，第二级或高级制冷循环冷却低级热泵流体，并可任选作进行天然气原料的初冷。低级制冷循环冷却并液化冷后的天然气原料，本方法的改进之处是利用一条吸收制冷循环以预冷天然气原料、低级热泵流体和高级热泵流体。最佳的吸收制冷循环是氨-水吸收制冷循环。使吸收制冷循环运转的热量可由方法中压缩机的一个或多个传动装置的废气来供给。
联系已知技术的典型天然气液化方法可很清楚地理解本发明。图1表示了这样一种液化方法。参见图1，通过管路12将天然气原料送进干燥器18中以除掉杂质，杂制在低温液化温度下将会结冰。现已知有多种类型的干燥器，它们均可在本发明中使用。然后，将干燥后的天然气经管路22任意地送到高级制冷热交换器24里，在其中天然气被初步地冷却。经初步冷却的天然气再经管路26送到低级制冷热交换器68中，在其中天然气得到进一步冷却并冷凝（液化）。在热交换器68中，管路26中的天然气原料和管路38中的深度闪蒸再循环气流混合而形成液态天然气。
然后这种液态天然气经管路28送到深度闪蒸体系30中，在其中这种液态天然气经两步被闪蒸而生成两种塔顶闪蒸气。塔顶闪蒸气经加热和压缩，一部分压缩后的闪蒸气被用作工艺压缩的燃料，其余部分称之为深度闪蒸气的压缩闪蒸气将通过交换器24和68连续冷却使其冷却和液化。通过管路40从深度闪蒸体系30中取出闪蒸气流的液态部分则为液态天然气产品。
高级制冷热交换器24的冷却是由一种混合的组合组分（多组分）制冷剂或单组分制冷剂闭合循环所提供的。高级制冷剂在压缩机76中被压缩，这种制冷条件可以变化，如图1管路70、72和74所示。随不同条件，压缩机76可以是单级压缩机或多级压缩机。压缩后的高级制冷剂经冷却后在分离器84中进行相分离而形成一种塔顶气流和一种液体。分离器84的塔顶气流经管路86送入压缩机88中压缩，然后经管路90送入高级制冷阶式环路98中。而液体通过管路96送到高级制冷阶式环路98中。在高级制冷阶式环路98中，混合的制冷剂作用产生制冷过程使干燥的天然气原料得到预冷和使低级制冷剂得到冷却。其后，用过的混合制冷剂再循环返回压缩机76中从而构成闭合循环。
低级制冷热交换器68的制冷过程是由一个混合制冷闭合循环所提供的。在该环路中，多组分制冷剂经管路50在压缩机52和54中被压缩。然后经压缩的低级制冷剂通过管路56送到热交换器24中进行冷却，并在其中被部分地冷凝。将这种冷凝的多组分制冷剂在分离器62中进行相分离。分离器62中的塔顶馏份和塔釜残液分别通过管路64和66送到低级制冷热交换器68中从而产生制冷过程，分别使管路26和38中的天然气原料和深度闪蒸再循环气流液化，然后，用过的塔顶和塔釜馏份再混合回到管路50中而构成闭合循环。
为进一步了解本发明，图1的方法经改进包括了一个吸收制冷循环则成为本发明的方法。这种经改进的方法如图2所示。在图2中，相似于图1的工艺的气流和装置以相同的数字表示。参见图2中的改进处，吸收制冷循环分别使得天然气流在干燥之前（管路12）、低级制冷剂在交换器24中与高级制冷剂热交换之前（管路56）、深度闪蒸再循环气在交换器24中与高级制冷剂热交换之前（管路32）、压缩后的高级制冷剂相分离之前（管路78）和压缩后的高级制冷剂塔顶馏份送入交换器24之前（管路90）达到初步预冷。这些预冷分别在热交换器14、58、34、80和92中进行。该方法其余部分与图1相同。
为更好地说明吸收制冷循环和图2方法之间的关系，而绘制了图3。图3表示一个标准的氨-水吸收制冷循环。参见图3，制冷循环中压缩机的传动装置排放的废热通过管路100送到热交换器102中，在其中废热加热并气化从氨-水蒸馏柱108中得到的部分在104管路中的塔釜液流。温热的蒸气通过管路106重新回到柱108中，柱108的塔顶气流通过管路110引出并冷却、冷凝同时分成两部分。一部分经管路114与经管路128得到的分离器118塔釜液流混合送到柱108顶部作回流液。另一部分通过管路116经低温冷却、闪蒸并在分离器118中进行相分离。
分离器118中的塔釜液流经管路120取出并分成较多的和较少的两部分。较少部分液流经管路124送入泵126中增压，然后经管路128与管路与管路114中的塔顶冷凝液流相混合。管路112中的较多部分液流将分成5小份，将其中1小份液流130送到热交换器14中以预冷管路12中的天然气原料;1小份液流132送到热交换器34中以预冷管路32中的深度闪蒸再循环气流;1小份液流134送到热交换器58中以预冷管路56中的经压缩的低级制冷剂;1小份液流136送到热交换器80中以预冷管路78中的经压缩的高级制冷剂;最后1小份138送到热交换器92中以冷却管路90中的经压缩的高级塔顶馏份。管路140、142、144、146和148中受热后的液流重新混合并经管路150送到相分离器118中。
交分离器118中的塔顶馏份经管路168取出并与管路166中的受热后的闪蒸塔釜液流相混合而形成液流170。闪蒸的塔釜液流是经管路160从柱108而来的塔釜液流的一部分，它先在热交换器162中受热并通过阀164闪蒸。液流170经冷却后在泵172中增压并分成为两份中间再沸液流，管路176中的头一份中间再沸液流在热交换器162中冷却，然后经管路178引到柱108的底部。第二份中间再沸液经管路180加到柱108的中部。
为证实本发明方法的效能和益处，将图1和图2的方法进行计算机拟。表Ⅰ列出了两种方法有关参数的比较值。
表Ⅰ
参数    图1方法    图2方法
LNG产量：MMSCFD    340.0    381.84
压缩机功率：Hp
低级循环    56，390    55，020
高级循环    57，527    54，588
深度闪蒸：11，647    11，554
总计    125，564    121，162
单位功率：Hp/MMSCFD    369.3    317.3
混合制冷剂组合物：%
表Ⅰ（续）
参数    图1方法    图2方法
高级：
C11.1 1.1
C238.9 50.0
C360.0 48.9
低级：
N20.2 0.0
C145.7 43.5
C248.7 56.5
C35.4 0.0
交换器UA×1E6
高级总计    51.57    50.78
低级总计    38.84    29.50
可利用的废热：MMBTU/hr    709.2    609.4
吸收再沸器效率：MMBTU/hr    0.0    461.9
末利用的废热：MMBTU/hr    709.2    147.5
从上表可见，就每种方法的单位功率而言，本发明的方法比先有技术的方法有较高的能量效率，约高16.4%。应该注意，这并非将全部废热都利用起来，若全得到利用，则可进一步获得改善。
为了把本发明的方法与其它先有技术的方法作进一步比较，下面列出表Ⅱ。在表Ⅱ中列出了几种先有技术的方法以及它们在相同能耗下（按输入燃气透平计）的生产能力。
表Ⅱ
方法    生产能力%
图1    104
图2    121
美国专利3，817，046    107
美国专利3，763，658    100
美国专利4，525，795    104
美国专利4，545，795    104
从表中可见，图2的方法，也就是本发明的方法其能量效率高于先有技术的任一方法。
最后，本发明的方法除了在没有使用辅助燃料提高了能量效率之外，还有其它一些显著的优点，其中有在该方法的某些区域能控制温度以便克服水合物的形成;高级预冷压缩机释放的压力稳定（即随室温变化预冷温度恒定）;机械能利用和分配灵活（即一定数目和大小的压缩装置能极大地提高其生产能力），同时能容易地改造翻新成两条闭合循环液化装置以增加产量。
经参照具体的实施例已对本发明的方法作了叙述，但这些实施例不应视为是对本发明的范围的限制。本发明的范围由下述权利要求书所确定。

Claims (10)

1、一种液化天然气的方法，其中，天然气原料得到冷却和液化；这种液化方法的制冷过程是由两条闭合制冷循环所提供的；以混合的(多组分)制冷剂为热泵流体的初级或低级制冷循环冷却并液化天然气原料；以混合的(多组合)制冷剂或单组分制冷剂为热泵流体的第二级或高级制冷循环冷却低级热泵流体；提高该方法的能量效率的改进处包括装一有条吸收制冷循环以预冷天然气原料、低级热泵流体和高级热泵流体。
2、一种液化天然气的方法，其中，天然气原料得到冷却和液化;这种液化方法的制冷过程是由两条闭合制冷循环所提供的;以混合的（多组分）制冷剂为热泵流体的初级或低级制冷循环冷却并液化天然气原料;以混合的（多组合）制冷剂或单组分制冷剂为热泵流体的第二级或高级制冷循环冷却低级热泵流体;至少将液化的天然气一部分进行闪蒸从而形成闪蒸气流;至少有一部分的闪蒸气流再被压缩并再循环返回方法中作深度闪蒸液;提高该方法能量效率的改进处包括装有一条吸收制冷循环以预冷天然气原料、低级热泵流体、高级热泵流体和深度闪蒸液。
3、如权利要求1所述的一种方法，其中，吸收制冷循环是氨-水吸收制冷循环。
4、如权利要求2所述的一种方法，其中，吸收制冷循环是氨-水吸收制冷循环。
5、如权利要求1所述的一种方法，该方法进一步包括以低级制冷循环冷却天然气原料之前先用高级制冷循环冷却天然气原料。
6、如权利要求2所述的一种方法，该方法进一步包括以低级制冷循环冷却天然气原料之前先用高级制冷循环冷却天然气原料。
7、如权利要求1所述的一种方法，其中单组分热泵流体是丙烷。
8、如权利要求2所述的一种方法，其中单组分热泵流体是丙烷。
9、如权利要求1所述的一种方法，其中在低级和高级制冷循环中压缩低级和高级热泵流体的能量是由气体透平机的废气所供给的，并利用从压缩系统回收的废能来驱动吸收制冷循环。
10、如权利要求2所述的一种方法，其中在低级和高级制冷循环中压缩低级和高级热泵流体的能量是由气体透平机的废气所供给的，并利用从压缩系统回收的废能来驱动吸收制冷循环。
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CN100552322C (zh) * 2007-10-10 2009-10-21 中国船舶重工集团公司第七一一研究所 带喷射器的中小型混合工质天然气液化制冷循环系统
CN101614464B (zh) * 2008-06-23 2011-07-06 杭州福斯达实业集团有限公司 高低温氮气双膨胀天然气液化方法
CN101880560A (zh) * 2009-05-05 2010-11-10 气体产品与化学公司 预冷却的液化方法
CN101644527B (zh) * 2009-08-26 2011-12-28 四川空分设备(集团)有限责任公司 天然气液化工艺的制冷系统和液化系统
CN103322727A (zh) * 2012-03-20 2013-09-25 北京科技大学 一种热泵系统及干燥系统以及方法
CN103322727B (zh) * 2012-03-20 2015-08-12 北京科技大学 一种热泵系统及干燥系统以及方法
CN102620460A (zh) * 2012-04-26 2012-08-01 中国石油集团工程设计有限责任公司 带丙烯预冷的混合制冷循环系统及方法
CN102927791A (zh) * 2012-11-30 2013-02-13 中国石油集团工程设计有限责任公司 带预冷的双复合冷剂制冷系统及方法
CN110573814A (zh) * 2016-12-22 2019-12-13 前苏伊士环能集团 用于液化天然气的设备和方法及包括该设备的船

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