CN101743430A - 蒸发气体处理方法及处理系统 - Google Patents

蒸发气体处理方法及处理系统 Download PDF

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CN101743430A
CN101743430A CN200880024213A CN200880024213A CN101743430A CN 101743430 A CN101743430 A CN 101743430A CN 200880024213 A CN200880024213 A CN 200880024213A CN 200880024213 A CN200880024213 A CN 200880024213A CN 101743430 A CN101743430 A CN 101743430A
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gas
outlet
steam distillation
boil
compressor
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CN101743430B (zh
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保罗·布里奇伍德
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Lng Technology Co Ltd
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LNG Technology Pty Ltd
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Abstract

提供了一种用于在低温液体贮罐和低温液体接收/装载设备之间输送低温液体的流送管系统，以及一种在低温液体贮罐和低温液体接收/装载设备之间输送低温液体期间将所述系统维持在低温温度或者稍微高于低温温度的方法。该流送管系统具有主输送导管和与低温液体贮罐和低温液体接收/装载设备流体连通的蒸汽回流管线。提供了冷却介质管线，其与主输送导管、蒸汽回流管线和冷蒸发气体源流体连通，其中冷蒸发气体处于或稍微高于低温温度。在低温液体输送期间，冷蒸发气体通过主输送导管和蒸汽回流管线在所述贮罐和所述设备之间循环，以将主输送导道和蒸汽回流管线维持在低温温度或稍微高于低温温度。

Description

蒸发气体处理方法及处理系统
技术领域
本发明涉及一种处理低温液体贮罐中的蒸发气体的方法和系统，例如LNG或者NGL贮罐中的液化气体。
发明内容
低温温度气体的液化典型地需要制冷源，例如混合有丙烷的制冷剂或阶流式制冷装置。特别是，闭环单一混合制冷剂特别适于用在液化装置中以处理天然气或煤层瓦斯(CSG)。发明人已经认识到，通过将低温贮罐中产生的蒸发气体重新引导至制冷装置，并将所述气体液化以重新获得被进一步液化的甲烷和具有烃组分的气体分馏物，可以增加LNG的产量和在液化装置中获得额外的效率，进一步液化的甲烷和具有烃组分的气体分馏物更适于用作燃气或再生气体以向液化设备中的各个部件提供能量。
因此，本发明的第一个方面提供了一种方法，其用于处理低温液体贮罐中产生的蒸发气体，包括下列步骤：
a)压缩所述蒸发气体；
b)以一种方式冷却压缩蒸发气体以产生液体分馏物和冷蒸汽分馏物；
c)分离所述液体分馏物和所述冷气体分馏物；以及
d)将所述液体分馏物重新引导至所述低温液体贮罐。
在本发明一个实施例中，所述蒸发气体被压缩到压力为约3巴到约6巴。
在本发明一个实施例中，冷却所述压缩蒸发气体的所述步骤包括使所述压缩蒸发气体通过制冷区域。优选地，冷却所述压缩蒸发气体的所述步骤包括使所述压缩蒸发气体流动与混合制冷剂进行逆流热交换。
在本发明优选实施例中，将所述液体分馏物和所述冷蒸汽分馏物冷却至所述低温液体贮罐的存储物的温度或者稍微高于所述低温液体贮罐的存储物的温度。具体地，所述液体分馏物和所述冷蒸汽分馏物被冷却至低温温度。
在另一实施例中，所述冷蒸汽分馏物被至少部分去除了包含在所述液体分馏物中的物质。具体地，所述液体分馏物主要包括具有一些氮气的液态甲烷，且冷蒸汽分馏物主要包括具有一些甲烷的氮气。
有利的是，该方法提供了从所述液体分馏物排除氮气，使得蒸汽分馏物的氮气的浓度相对于液体分馏物的氮气的浓度增加。
在本发明又一实施例中，所述方法还包括将所述冷蒸汽分馏物压缩到适于用作燃气和/或再生气体的压力。
所述冷蒸汽分馏物被压缩到需要的燃气压力。在本发明优选实施例中，所述冷蒸汽分馏物用作燃气以驱动所述液化装置中的一个或多个压缩机。
本发明的第二个方面，提供一种系统，其用于处理在低温液化贮罐中产生的蒸发气体，其包括：
低温液化贮罐，其具有蒸发气体出口和液体入口；
第一压缩机，其具有出口和与所述蒸发气体出口流体连通的入口；
制冷区域，其具有出口和与所述第一压缩机的所述出口流体连通的入口，所述制冷区域被设置以冷却压缩的气体并产生液体分馏物和冷蒸汽分馏物；
分离器，其具有与所述制冷区域的所述出口流体连通的入口、冷蒸汽分馏物出口和液体分馏物出口；和
管线，其与所述分离器的所述液体分馏物出口和所述低温液体贮罐的所述液体入口流体连通。
在另一实施例中，本发明的所述系统还包括：
第二压缩机，其具有出口和与所述分离器的所述冷蒸汽分馏物出口流体连通的入口；和
管线，其与所述第二压缩机的所述出口和再生气体/燃气系统流体连通。
优选地，所述第一压缩机为低压压缩机，所述第二压缩机为高压压缩机。
在本发明一个实施例中，所述制冷区域用在液体材料液化装置中。在一个优选实施例中，所述制冷区域包括单一混合制冷剂装置。
附图说明
现在参照所附附图仅通过示例方式描述包括本发明的各个方面的优选实施例，其中：
图1是用于液化例如天然气或者CSG的流体材料的方法示意流程图，其中该流程图也包括根据本发明一个实施例处理低温液体贮罐中的蒸发气体的方法；和
图2是单一混合制冷剂和流体材料的组分冷却和加热曲线。
具体实施方式
参照图1，其示出将流体材料冷却到低温温度的方法，以达到将其液化的目的。流体材料的描述性示例包括但不限于天然气和煤层瓦斯(CSG)。尽管本发明的具体实施例被描述为涉及从天然气或CSG生产液化天然气(LNG)，但可以预想到该方法可应用到在低温温度下可被液化的其它流体材料。
通过预处理天然气或CSG供给气体以移除水、二氧化碳和当接近液化温度时在下游可凝固的可选的其它种类物质，然后将预处理过的供给气体冷却至产生LNG的低温温度，从而广泛实现LNG的生产。
参照图1，供给气体60在大约900磅/平方英寸(psi)的控制压力下进入处理过程。通过使该供给气体通过传统的密封式二氧化碳汽提装置62而将二氧化碳从该供给气体中移除，其中根据供给气体10的二氧化碳的浓度移除二氧化碳使之达到大约百万分之50-150(50-150ppm)。二氧化碳汽提装置62的示例包括具有胺接触器(例如MDEA)和胺再沸器的胺包。典型地，从胺接触器出来的气体充满了水(例如，～701b/MMscf)。为了去除大量的水，利用冷冻器66提供的冷冻水将气体冷却至其液化点(例如，～15℃)。优选地，冷冻器66利用辅助制冷系统20的制冷能力。冷凝的水从冷却气流中被移除并回到胺包以构成。
液化之前必须将水从冷却气流中移除使之小于等于1ppm，以避免当气流温度降低到低于液化冰点时结冰。因此，具有减少的含水量(例如，-201b/MMscf)的冷却气流被输送到脱水装置64。脱水装置64包括三个分子筛容器。典型地，两个分子筛容器工作在吸附模式下，第三个过滤器为再生模式或备用模式。从运行容器中出来的干燥气体的支流被用于再生气体。通过使用空气冷却湿润的再生气体，压缩的水被分离出来。饱和气流被加热并用作燃气。蒸发气体(BOG)优选用作再生气体/燃气(如将在后面描述的那样)，且任何不足之量由干燥气流供给。不需要循环压缩机用于再生气体。
尽管应该认识到很多硫化合物目前可通过二氧化碳汽提装置62中的二氧化碳被移除，供给气体60可选地可经过进一步的处理以移除其它含硫物质或类似物，例如硫化合物。
预处理的结果是，供给气体60变热其温度高达50℃。在本发明的一个实施例中，预处理过的供给气体可选地可通过冷冻器(未显示)被冷却至大约10到-50℃的温度。在本发明的过程中可使用的冷冻器的合适的示例包括但不限于氨吸收冷冻器、溴化锂吸收冷冻器及其类似物、或者辅助制冷系统20。
有利地，根据供给气体的组分，冷冻器可浓缩预处理过的气流中的重烃。这些浓缩的组分能够形成额外的产物流，或者可在系统各个部件中用作燃气。
与现有技术相比，冷却预处理过的气流的主要优点在于显著地减少了液化所需的冷却工作量，在一些情况下减少了多达30％。
冷却的预处理过的气流通过管线32供给到制冷区域28，在制冷区域所述气流被液化。
制冷区域28包括热交换机，由混合制冷剂在热交换机中提供制冷。优选地，热交换机包括封闭在净化钢箱中的黄铜铝盘鳍管热交换芯。
制冷热交换机具有与压缩机12流体连通的第一热交换通道40，第二热交换通道42和第三热交换通道44。第一、第二和第三热交换通道40、42、44中的每一个延伸通过制冷热交换机，如图1所示。制冷热交换机还设置有第四热交换通道46，其延伸通过制冷热交换机的一部分，尤其是制冷热交换机中的较冷部分。第二和第四热交换通道42、46被定位为相对于第一和第三热交换通道40、44逆流热交换。
通过在制冷区域28循环混合的制冷剂而向制冷区域28提供制冷。来自制冷剂抽引室10的混合制冷剂被传送到压缩机12。压缩机12优选为两个平行的单级离心压缩机，每个直接由气体涡轮机100驱动，尤其是空气诱导气体涡轮机。可替换地，压缩机12可以是具有中间冷却器和级间涤气器的两级压缩机。典型地，压缩机12是工作效率为大约75％到85％的类型。
气体涡轮机100的废热可被用于产生气流，该气流反过来被用于驱动发电机(未显示)。采用这种方式，可以产生足够的电能以向液化装置中的所有电子元件提供电流。
气体涡轮机100的废热产生的气流还可被用于加热二氧化碳汽提装置62的胺再沸器，用于脱水装置64的分子筛的再生、再生气体和燃气。
混合制冷剂被压缩到压力大约为30巴到50巴，且典型地压缩到压力大约为35巴到40巴。在压缩机12中压缩的结果导致压缩的混合制冷剂的温度升高至大约120℃到大约160℃的温度，且典型地升高到大约140℃。
然后，压缩的混合制冷剂通过管线14被输送到冷却器16，以将压缩的混合制冷剂的温度降低到低于45℃。在一个实施例中，冷却器16为气冷鳍管热交换机，通过使压缩的混合制冷剂相对于诸如空气或类似物的流体以逆流形式通过而冷却压缩的混合制冷剂。在可替换实施例中，冷却器16为列管式热交换机，通过使压缩的混合制冷剂相对于诸如水或类似物的流体以逆流形式通过而冷却压缩混合制冷剂。
冷却的压缩混合制冷剂被输送到制冷区域28的第一热交换通道40，在此处其被进一步冷却且优选利用焦耳-汤姆森(Joule-Thomson)效应被膨胀器48膨胀，从而作为混合制冷冷冻剂向制冷区域28提供冷却。混合制冷冷冻剂被输送通过第二热交换通道42，此处，混合制冷冷冻剂通过与分别流经第一和第三热交换通道40、44的压缩混合制冷剂和预处理过的供给气体进行逆流热交换而被加热。然后，混合制冷气体在进入压缩机12之前回到制冷剂抽引室10，从而完成一个闭环单一混合制冷过程。
混合制冷构成由流体材料或蒸发气体(甲烷和/或C2-C5烃)、具有来源于外部的任一或者更多制冷组分的氮气发生器(氮气)提供。
混合制冷剂包含选自由氮气和包含1个到大约5个碳原子的烃组成的组中。当待被冷却的流体材料为天然气或煤层瓦斯时，用于混合制冷剂的合适的组分具有下列摩尔百分含量范围：氮气：大约5到大约15；甲烷：大约25到大约35；C2：大约33到大约42；C3：0到大约10；C4：0到大约20；和C5：0到大约20。在优选实施例中，混合制冷剂包括氮气、甲烷、乙烷或乙烯，以及异丁烷和/或n-丁烷。
图2示出单一混合制冷剂和天然气的组分冷却和加热曲线。曲线基本接近在大约2℃以内，表明了本发明方法和系统的效率。
通过辅助制冷系统20可以向制冷区域28提供额外的制冷。辅助制冷系统20包括一个或多个由空气冷却器冷却的胺制冷包。例如较冷的氨水的辅助冷却剂被输送通过位于制冷区域28较冷区域中的第四热交换通道44。通过这种方法，辅助制冷系统20可利用的高达大约70％的冷却效率将被用于制冷区域28。额外的冷却致使可额外生产20％的LNG，且也改进装置效率，例如气体涡轮机100中的燃料消耗单独减少20％。
辅助制冷系统20利用来自气体涡轮机100的热排出气体产生的废热，为辅助制冷系统20产生制冷。但是，可以理解的是，由液化装置中其它部件产生的额外废热也可用于为辅助制冷系统20再次产生制冷，例如来自其它压缩机、动力产生装置使用的原动机、热的照明气体、废气或流体、太阳能和类似物。
辅助制冷系统20还可用于冷却气体涡轮100的入口空气。重要的是，当压缩机输出与LNG输出大致成正比时，冷却气体涡轮的入口空气将使装置增加15-25％的产出率。
通过温度为大约150℃到大约-160℃的管线72，在制冷区域28重新获得液化气体。液化的气体然后通过膨胀器74膨胀，结果导致液化的气体的温度降低至大约-160℃。在本发明中可使用的膨胀器的合适的示例包括但不仅限于膨胀阀、JT阀、文氏管设备和旋转机械膨胀器。
然后，通过管线78将液化的气体引导至贮罐76。
贮罐76中产生的蒸发气体(BOG)可通过管线80充入优选为低压压缩机的压缩机78。压缩的BOG通过管线82被供给到制冷区域28，且被输送通过制冷区域28的一部分，在该部分所述压缩BOG被冷却到大约-150℃到-170℃的温度。
在这些温度下，BOG的一部分被浓缩成液相。特别地，液相的冷却BOG主要包括甲烷。虽然气相的冷却BOG也包括甲烷，但是与液相相比，气相的氮气浓度增加，典型地为大约20％到60％。所述气相最终组分适宜于用作燃气。
最终的两相混合物通过管线86被输送到分离器84，在经过分离器84之后，其中分离的液相物质通过管线88被重新引导回贮罐76。
在分离器84中分离的冷却气相物质通过管线被输送到压缩机，优选为高压压缩机，且在装置中用作燃气和/或再生气体。
可替换地，在分离器84中分离的冷却气相物质适于用作冷却介质，循环经过用于从贮罐76向接收/加载设备输送例如LNG或煤层瓦斯的液态甲烷的低温流送管系统，从而将流送管系统维持在低温温度或者稍微高于低温温度。
可以理解的是，尽管本文参考现有技术的使用和公开出版物，但这些参考并不是承认这些参考中的任何参考会形成在澳大利亚或者任何其它国家的公知技术。
为了说明的目的，应该清楚地理解单词“包括(comprising)”指的是“包括但不仅限于”，以及单词“包括(comprises)”具有相应的含义。
除了已经描述的部分以外，在不背离本基本发明思想的情况下，本领域技术人员可想到各种变型和修改。所有这些变型和修改应该被认为落入本发明的范围内，本发明的本质可从前面描述中确定。
例如，尽管上述本发明的特定实施例涉及煤层瓦斯的天然气中的LNG的液化，但是本发明可以容易地用于涉及低温温度下液态存储的其它气体。

Claims (17)

1.一种方法，其用于处理低温液体贮罐中产生的蒸发气体，包括以下步骤：
a)压缩所述蒸发气体；
b)以一种方式冷却压缩蒸发气体以产生液体分馏物和冷蒸汽分馏物；
c)分离所述液体分馏物和所述冷气体分馏物；以及
d)将所述液体分馏物重新引导至所述低温液体贮罐。
2.如权利要求1所述的方法，其中所述蒸发气体被压缩到压力为约3巴到约6巴。
3.如权利要求1或2所述的方法，其中冷却所述压缩蒸发气体的所述步骤包括使所述压缩蒸发气体通过制冷区域。
4.如权利要求3所述的方法，其中冷却所述压缩蒸发气体的所述步骤包括使所述压缩蒸发气体流动与混合制冷剂进行逆流热交换。
5.如权利要求4所述的方法，其中所述混合制冷剂是单一混合制冷剂。
6.如权利要求1至5中任一项所述的方法，其中将所述液体分馏物和所述冷蒸汽分馏物冷却至所述低温液体贮罐的存储物的温度或者稍微高于所述低温液体贮罐的存储物的温度。
7.如权利要求6所述的方法，其中所述液体分馏物和所述冷蒸汽分馏物被冷却至低温温度。
8.如权利要求1至7中任一项所述的方法，其中所述冷蒸汽分馏物被至少部分地去除了包含在所述液体分馏物中的物质。
9.如权利要求1至8中任一项所述的方法，其中所述液体分馏物主要包括液体甲烷。
10.如权利要求1至9中任一项所述的方法，其中所述蒸汽分馏物中的氮气的浓度大于所述液体分馏物中的氮气的浓度。
11.如权利要求1至10中任一项所述的方法，其中所述冷蒸汽分馏物包括至少50％的氮气。
12.如权利要求1至11中任一项所述的方法，其中所述方法进一步包括将所述冷蒸汽分馏物压缩到适于用作燃气和/或再生气体的压力。
13.如权利要求1至12中任一项所述的方法，其中所述冷蒸汽分馏物用作燃气以驱动所述液化装置中的一个或多个压缩机。
14.一种系统，其用于处理在低温液化贮罐中产生的蒸发气体，该系统包括：
低温液化贮罐，其具有蒸发气体出口和液体入口；
第一压缩机，其具有出口和与所述蒸发气体出口流体连通的入口；
制冷区域，其具有出口和与所述第一压缩机的所述出口流体连通的入口，所述制冷区域被设置以冷却压缩的气体并产生液体分馏物和冷蒸汽分馏物；
分离器，其具有与所述制冷区域的所述出口流体连通的入口、冷蒸汽分馏物出口和液体分馏物出口；和
管线，其与所述分离器的所述液体分馏物出口和所述低温液体贮罐的所述液体入口流体连通。
15.如权利要求14所述的系统，其中所述系统进一步包括：
第二压缩机，其具有出口和与所述分离器的所述冷蒸汽分馏物出口流体连通的入口；和
管线，其与所述第二压缩机的所述出口和再生气体/燃气系统流体连通。
16.如权利要求15所述的系统，其中所述第一压缩机为低压压缩机，所述第二压缩机为高压压缩机。
17.如权利要求14至16中任一项所述的方法，其中所述制冷区域用在液体材料液化装置中。
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