CN107339853A - 天然气液化系统和方法 - Google Patents

天然气液化系统和方法 Download PDF

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Publication number
CN107339853A
CN107339853A CN201611162705.9A CN201611162705A CN107339853A CN 107339853 A CN107339853 A CN 107339853A CN 201611162705 A CN201611162705 A CN 201611162705A CN 107339853 A CN107339853 A CN 107339853A
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China
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gas
feed gas
produce
cooling
phase components
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CN201611162705.9A
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CN107339853B (zh
Inventor
吉川喜次
酒井功朗
酒井功一朗
提姆·张
刘育南
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Hercules Engineering LLC
Chiyoda Corp
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Chiyoda Chemical Engineering and Construction Co Ltd
Air Products and Chemicals Inc
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F25J3/0214—Liquefied natural gas
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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Abstract

通过使用由原料气体的膨胀使膨胀机产生的动力，增大压缩机的出口压力，并降低对于冷却器的冷却容量的要求。天然气液化系统(1)包括：第一膨胀机(3)，其用于通过使用压力状态下的天然气作为原料气体来产生动力；第一冷却单元(11，12)，其用于冷却在所述第一膨胀机中通过膨胀减压的所述原料气体；蒸馏单元(15)，其用于通过蒸馏由所述第一冷却单元冷却的所述原料气体来减少或除去所述原料气体中的重质组分；第一压缩机(4)，其用于通过使用在所述第一膨胀机中所产生的动力来压缩通过所述蒸馏单元从其中减少或除去所述重质组分的所述原料气体；以及液化单元(21)，其用于通过与制冷剂进行热交换来液化由所述第一压缩机压缩的所述原料气体。

Description

天然气液化系统和方法
本申请为专利申请201480071324.2的分案申请，原申请的申请日为2014年12月26日，发明创造名称为天然气液化系统和方法。
技术领域
本发明涉及一种用于通过冷却天然气产生液化天然气的天然气液化系统和方法。
背景技术
从天然气田获得的天然气在液化工厂中液化，从而天然气可以以液体形式被存储和运输。当冷却至约-162摄氏度时，相比于气态天然气，所述液体天然气具有显著减小的体积，且不需要在高压下存储。同时天然气液化过程中除去包含在开采的天然气中的杂质，例如水、酸性气体和汞，并且在除去具有相对高的凝固点的较重组分后(如苯、戊烷的C5+烃类和其他更重的烃类)，所述天然气被液化。
已经开发了用于液化天然气的各种技术，其中包括那些基于使用膨胀阀和涡轮机的膨胀过程和使用低沸点制冷剂(例如轻质烃，如甲烷、乙烷和丙烷)的热交换过程的技术。例如，某个已知的天然气液化系统(参照专利文献1)包括用于冷却天然气的冷却单元，其中从所述冷却单元中除去杂质；膨胀单元，其用于等熵膨胀所述冷却的天然气；蒸馏单元，其用于蒸馏由所述膨胀单元以低于甲烷和较重的内容物的临界压力的压力减压的所述天然气；压缩机，其用于通过使用来自膨胀机的轴的输出来压缩来自所述蒸馏单元的所述蒸馏的天然气；以及液化单元，其用于通过与混合的制冷剂进行热交换来液化由压缩机压缩的所述蒸馏的天然气。
现有技术文件
专利文件0004
专利文献1：US4,065,278
发明内容
本发明要完成的课题
在如专利文献1中所公开的常规的天然气液化系统，希望所述压缩机的出口压力(或待被引入所述液化单元的进料气体的压力)是尽可能的高的，从而降低液化单元(尤其是，所述液化单元的主热交换器)上的负荷，并且最大化所述液化工艺的效率。
为了增加所述压缩机的所述出口压力时，需要相应大的动力。然而，在常规装置中，其中由冷却单元冷却的所述进料气体通过膨胀机膨胀，由膨胀机产生的动力是有限的，并且不足以将所述压缩机的所述出口压力提高到所需水平。
在常规装置中，由于需要使进料气体在膨胀机中被膨胀之前被冷却，所述冷却单元需要相对大的容量，而这增加了所述冷却单元的初始成本和运营成本。
在常规装置中，因为进料气体的冷却会导致产生冷凝物，有必要提供一种气液分离器，在将所述进料气体从所述冷却单元引入所述膨胀机之前，从进料气体中分离(除去)冷凝物。此外，由于在压缩机的出口端，所述进料气体温度高，则所述液化单元的中间入口点与制冷剂之间产生显著的温差，从而所述冷却单元需要相应大的容量。
鉴于现有技术的这些问题，本发明的一个主要目的在于提供一种天然气液化系统和方法，通过使用由所述进料气体的膨胀在膨胀机中所产生的动力来增加所述压缩机的出口端的压力，并最大限度地减少所述冷却单元所需的冷却容量。
完成所述课题的手段
本发明的第一个方面提供一种天然气液化系统(1)，其冷却所述天然气以产生液化天然气，包括：第一膨胀机(3)，其用于通过膨胀加压状态下的天然气作为原料气体来产生动力；第一冷却单元(11，12)，其用于冷却在所述第一膨胀机中通过膨胀减压的所述原料气体；蒸馏单元(15)，其用于通过蒸馏由所述第一冷却单元冷却的所述原料气体来减少或除去所述原料气体中的重质组分；第一压缩机(4)，其用于通过使用在所述第一膨胀机中所产生的动力来压缩所述原料气体，其中通过所述蒸馏单元从所述原料气体中减少或除去所述重质组分；第二换热器，其用于在被引入第一压缩机的所述原料气体和由第一压缩机压缩的所述原料气体之间进行热交换；以及液化单元(21)，其用于通过与制冷剂进行热交换来液化由所述第一压缩机压缩的所述原料气体。
根据本发明的第一方面，由于利用被所述第一冷却单元冷却之前的所述原料气体的膨胀所产生的动力，从而可使所述第一压缩机的出口压力增加，降低所述第一冷却单元所需的冷却容量。
本发明的第二方面提供一种天然气液化系统，进一步包括热交换器(69)，其用于对被引入所述蒸馏单元的所述原料气体以及来自所述蒸馏单元的顶部馏分之间进行热交换。
根据本发明的第二方面，即使当被引入到所述液化单元的所述原料气体的温度低于适当的范围时，能够通过与被引入到所述蒸馏单元中的所述原料气体进行热交换来加热所述蒸馏单元的顶部馏分，从而使所述原料气体的温度接近所述蒸馏单元的入口端的温度。
本发明的第三方面提供一种天然气液化系统，进一步包括第二热交换器(79)，其用于对待被引入所述第一压缩机的所述原料气体以及由所述第一压缩机压缩的所述原料气体之间进行热交换。
根据本发明的第三方面，即使当被所述第一压缩机压缩并被引入到所述液化单元的所述原料气体的温度高于适当的范围时，能够通过与被引入到所述第一压缩机中的所述原料气体进行热交换来冷却来自所述第一压缩机中的所述原料气体，从而使所述原料气体的温度接近所述液化单元的入口端的温度。
发明效果
正如可从前述中所理解，根据本发明的天然气液化的液化系统，通过使用由原料气体的膨胀于所述膨胀机产生的动力，可使得所述压缩机的所述出口压力增加，并使得所述冷却单元所需的冷却容量减小。
附图说明
图1为示出作为本发明的第一实施例给出的所述天然气液化系统中的液化处理流程的示意图；
图2为示出作为第一比较例给出的常规天然气液化系统中的液化处理流程的示意图；
图3为示出作为第二比较例给出的常规天然气液化系统中的液化处理流程的示意图；以及
图4为示出作为第一实施例的第一变形例给出的一种天然气液化系统中的液化处理流程的示意图；
图5为示出作为第一实施例的第二变形例给出的一种天然气液化系统中的液化处理流程的示意图；
图6为示出作为第一实施例的第三变形例给出的一种天然气液化系统中的液化处理流程的示意图；
图7为示出作为第一实施例的第四变形例给出的一种天然气液化系统中的液化处理流程的示意图；
图8为示出作为本发明的第二实施例给出的一种天然气液化系统中的液化处理流程的示意图；
图9为示出作为第二实施例的第一变形例给出的一种天然气液化系统中的液化处理流程的示意图；
图10为示出第一实施例的第五变形例的所述天然气液化系统中的液化处理流程的示意图。
术语表
1 液化系统
2 除水单元
3，3a 第一膨胀机
3b 第二膨胀机
4，4a 第一压缩机
4b 第三压缩机
5 轴
10，11，12 第一冷却器
15 蒸馏单元
21 液化单元
23 第一气液分离容器
33 膨胀阀
41 制冷剂分离器
44 膨胀阀
45 喷头
54 膨胀阀
55 喷头
69 热交换器
79 热交换器
80 冷却器
Z1 暖区
Z2 中间区
Z3 冷区
具体实施方式
以下参照附图对本发明的优选实施例进行说明。
(第一实施例)
图1为示出作为本发明的第一实施例给出的所述天然气液化系统中的液化处理流程的示意图。将在下文示出的表1列出所述天然气液化系统中的液化过程的模拟(仿真)结果。表2至表12的内容也是如此。表1示出在第一实施例的液化系统中的每个不同点处，待液化的天然气的温度、压力、流速以及摩尔组成。在表1中，(i)至(ⅸ)列示出在液化系统1中用对应的图1中罗马数字(i)至(ix)表示的在各点处的值。
含有约80至98mol％的甲烷的天然气用作所述原料气体或所述进料气体。所述原料气体也至少包含至少0.1mol％的作为较重内容物的C5+烃类，或者至少包含至少1ppmmol的作为较重内容物的BTX(苯，甲苯，二甲苯)。非甲烷气体的所述原料气体的含量示于表1的列(i)中。根据液化的不同阶段，在本说明书中使用的术语“原料气体”并不一定需要为气态，但也可以是液态。
在此液化系统1中，所述原料气体经管路L1供应到除水单元2，并且并被除去水份以避免结冰的问题。供给到所述除水单元2的所述原料气体具有约20摄氏度的温度，大约kPaA的压力和大约00kg/hr的流速。所述除水单元2可以由填充有干燥剂(如分子筛)的多个塔构成，并可以将所述原料气体中的水含量降低到小于0.1ppmmol。所述除水单元2可以由任何其它已知的能够将所述原料气体的水除去至低于所需的水平的单元构成。
虽然这里省略了详细的讨论，液化系统1可以采用附加的已知设备，用于执行在所述除水单元2中的处理步骤之前的初步处理步骤，诸如用于除去天然气冷凝物的分离单元，用于除去如二氧化碳和硫化氢的酸性气体的酸性气体去除单元，以及用于除去汞的除汞单元。通常情况下，所述除水单元2接收原料气体，其中通过使用这些设备从原料气体中去除杂质。对供应到所述除水单元2中的所述原料气体进行预处理，使得二氧化碳(CO2)的含量小于50ppmmol，硫化氢(H2S)含量小于4ppmmol，硫含量小于20mg/Nm3，汞含量小于10ng/Nm3。
所述原料气体的来源可以不限于任何特定的来源，但也可以非排他性地在加压状态下从页岩气，致密砂岩气和煤炭头甲烷(coalheadmethane)中获得。所述原料气体不仅可以经由管道由诸如天然气田的来源供应，也可以由储存罐供应。
在所述除水单元2从所述原料气体除去水，将所述原料气体经由管路L2被转递到第一膨胀机3。所述第一膨胀机3由涡轮机组成，其用于减少供应给其的天然气的压力，并在等熵的条件下从天然气的膨胀中获得动力(或能量)。由于在所述第一膨胀机3中的膨胀步骤(第一膨胀步骤)，所述原料气体的压力和温度被降低。所述第一膨胀机3设有与第一压缩机4共同的轴5(将在下文讨论)，从而使得通过所述第一膨胀机3产生的动力可以用于向所述第一压缩机4提供动力。如果所述第一膨胀机3的旋转速度低于所述第一压缩机4的旋转速度，合适的增速齿轮单元可被放置在所述第一膨胀机3和所述第一压缩机4之间。所述第一膨胀机3将所述原料气体的温度和压力分别降低至约8.3摄氏度和大约kPaA。通常情况下，从所述第一膨胀机3排出的所述原料气体的压力在kPaA到kPaA(30barA到55barA)的范围内，或更优选在kPaA至kPaA(35barA至50barA)的范围内。
所述原料气体从所述第一膨胀机3经管路L3被转递至冷却器11。通过将另一个冷却器12连接到所述冷却器11的下游端形成冷却单元(第一冷却单元)。所述原料气体通过与制冷剂在第一冷却单元11，12中进行分阶段的热交换(第一冷却步骤)而冷却。已经由所述第一冷却单元11，12冷却的所述原料气体的温度在-20至-50摄氏度的范围内，或更优选地在-25至-35摄氏度的范围内。如果引入所述液化系统1中的所述原料气体(的压力)相对较高(例如，高于100barA)，因为在所述第一膨胀机3的出口的温度相对较低(例如，-30摄氏度)，可以省略所述第一冷却单元11，12。在所述蒸馏单元15的上游侧省略所述冷却单元的可能性同样适用于将在下文讨论的在图5至7中所示的多个实施例。
在本实施例中，使用C3-MR(丙烷(C3)预冷却的混合制冷剂)系统。在第一冷却单元11，12中通过使用丙烷作为制冷剂预冷却所述原料气体，并在之后将其过冷却至极低温度，用于在制冷循环中使用将在下文讨论的混合制冷剂下液化天然气。用于中压(MP)和低压(LP)的丙烷制冷剂(C3R)被用于在第一冷却单元11，12中在多个阶段(在所示实施例在两个阶段)中冷却所述原料气体。虽然在附图中未示出，第一冷却单元11，12形成包括用于丙烷制冷剂的压缩机和冷凝器的本身已知的制冷循环的一部分。
液化系统1不一定需要基于所述C3-MR系统，但除了其它的可能性之外，还可以使用级联系统，在所述级联系统中通过使用具有不同沸点的相应的制冷剂(如甲烷，乙烷和丙烷)，使用例如乙烷和丙烷的混合介质的用于初步冷却过程的DMR(双混合制冷剂)系统以及使用不同的混合制冷剂分别用于初步冷却、液化和过冷却的单个循环的MFC(混合流体级联系统)来形成多个单独的制冷循环。
所述原料气体从冷却器12经管路L4被转递至所述蒸馏单元15。所述原料气体在该点的压力借助所述第一膨胀机3以及其它可选的过程的膨胀，应低于甲烷和较重组分的临界压力。所述蒸馏单元15基本上由内部设置有多层架的用于去除所述原料气体中较重的内容物(蒸馏步骤)的蒸馏塔构成。由较重的内容物构成的液体经由连接到所述蒸馏单元15的蒸馏塔的底端的管路L5排出。经由所述管路L5从所述蒸馏单元15排出的所述由较重的内容物构成的液体具有大约177摄氏度的温度和约20,000kg/hr的流速。术语“较重的内容物”是指例如苯的具有高凝固点的组分和具有低沸点的例如C5+烃类的组分。所述管路L5包括再循环单元，所述再循环单元包括用于通过与蒸汽(或油)进行热交换来加热从所述蒸馏单元15的蒸馏塔的底部排出的液体的一部分的再沸器16,并将加热的液体再循环返回到所述蒸馏单元15，其中所述蒸汽(或油)从外部被提供给所述再沸器。
来自所述蒸馏单元15的顶部馏分由所述原料气体的较轻组分构成，所述较轻组分主要由具有低沸点的甲烷构成，并且所述原料气体通过管路L6被引入所述液化单元21中，以在管道系统22a和22b中冷却。转递到管路L5的所述原料气体具有大约-45.6摄氏度的温度和大约kPaA的压力。在蒸馏单元15中除去所述较重组分的所述原料气体含有少于0.1mol％的C5+和小于1ppmmol(苯，甲苯和二甲苯)的BTX。通过流经所述管道系统22a和22b，所述原料气体被冷却至大约-65.2摄氏度，然后从所述液化单元21经由管路L7转递到第一气液分离容器23。
如将在下文中讨论的，所述液化单元21基本上由所述液化系统1中的主热交换器构成，而此热交换器由线轴缠绕式热交换器构成，所述线轴缠绕式热交换器包括用于传导所述原料气体和制冷剂的传热管的外壳和线圈。所述液化单元21规定位于所述液化单元21下部的暖区Z1，其用于接收所述混合制冷剂并具有最高的温度(范围)；位于所述液化单元21中部的中间区Z2，其具有低于暖区Z1的温度；以及位于所述液化单元21上部的冷区，其用于排出所述液化的原料气体并具有最低的温度。在第一实施例中，所述暖区Z1由在较高温度侧的较高暖区Z1a和在较低温度侧的较低暖区Z1b组成。管道系统22a和22b，以及管道系统42a，51a，和42b和51b，分别由在较高暖区Z1a和较低暖区Z1b提供的管束形成，其中通过所述管道系统引导所述混合制冷剂。在所说明的实施例中，较高暖区Z1a的温度在待冷却的所述原料气体的上游侧(入口侧)为大约-35摄氏度，而在所述原料气体的下游侧(出口侧)为大约-50摄氏度。较低暖区Z1b的温度在所述原料气体的上游侧为大约-50摄氏度，而在所述原料气体的下游侧为大约-135摄氏度。中间暖区Z2的温度在所述原料气体的上游侧为大约-65摄氏度，而在所述原料气体的下游侧为大约-135摄氏度。冷区Z3的温度在所述原料气体的上游侧为大约-135摄氏度，而在所述原料气体的下游侧为大约-155摄氏度。各区域的在所述上游侧和下游侧的温度并不限于这里提到的数值，并且在每个部分的温度可以在预定的范围内变化((±例如5摄氏度)。
第一气液分离容器23分离所述原料气体的液相组分(冷凝物)，并且基本上由烃类构成的所述液体通过设置于管路L8的再循环泵24再循环返回所述蒸馏单元15。在第一气液分离容器23中得到的并主要由甲烷构成的所述气相组分经管路L9转递至第一压缩机4。所述原料气体以约0kg/hr的流速通过管路L8，并以约780,000kg/hr的流速通过管路L6。第一气液分离容器23也可以通过使用混合制冷剂或乙烯制冷剂冷却。
所述第一压缩机4由具有涡轮机叶片的用于压缩所述原料气体的单级离心式压缩机构成，其安装在与所述第一膨胀机3共有的轴5上。由所述第一压缩机4(第一压缩步骤)压缩的所述原料气体经管路L10引入所述液化单元21。由所述第一压缩机4输出到管路L10的所述原料气体具有约-51摄氏度的温度和约kPaA的压力。引入所述液化单元21的原料气体由所述第一压缩机4压缩，优选地压缩至超过至少kPaA的压力。
管路L10连接到位于所述液化单元21的所述暖区Z1b的管道系统30，所述管道系统30的上游端连接到所述中间区Z2中的管道系统31，然后连接到位于所述冷区Z3的管道系统32。所述天然气在通过流经所述管道系统31和32被液化并过冷却后，经由设置于管路L11的膨胀阀33被转递到在附图中未示出的用于存储目的的LNG储存罐。经受所述液化步骤的所述原料气体在所述膨胀阀33的下游端获得-162摄氏度的温度和大约120kPaA的压力。
流经所述液化单元21的所述原料气体，通过使用混合制冷剂的制冷循环冷却。在所说明的实施例中，所述混合制冷剂除了包括甲烷，乙烷和丙烷的烃类混合物，可各自含有氮气，但也可能有其他本身已知的只要所需的冷却容量可以实现的组合物。
在所述液化单元21中，高压(HP)混合制冷剂(MR)经由管路L12供应给制冷剂分离器41。组成所述制冷剂分离器41中的液相组分的所述混合制冷剂经由管路L13引入所述液化单元21，然后在所述液化单元21中向上流动通过分别位于暖区Z1a和Z1b的所述管道系统42a和42b，以及位于中间区Z2的所述管道系统43。所述混合制冷剂然后在设置于管路L14中的膨胀阀44中膨胀，并部分闪蒸。
在通过所述膨胀阀44后，所述混合冷冻剂从在中间区Z2的上部设置的喷头45向下喷出(以与所述液化单元21中的所述原料气体的流动相反)。从所述喷头45喷出的所述混合制冷剂向下流动，同时与由所述管道系统31，43和52(最后的管道系统将在下文中被讨论)形成的中间管束和由所述管道系统22a，22b，30，42a，42b，51a和51b(最后两个管道系统将在下文中被讨论)形成的下部管束进行热交换，所述管道系统31，43和52位于所述中间区Z2，所述管道系统22a，22b，30，42a，42b，51a和51b位于所述暖区Z1。
组成所述制冷剂分离器41中的气相组分的所述混合制冷剂经由管路L15引入所述液化单元21，然后在所述液化单元21中通过流经分别位于暖区Z1a和Z1b的所述管道系统51a和51b，流经位于所述中间区Z2的所述管道系统52，以及流经位于所述冷区Z3的所述管道系统53，向上流动。所述混合制冷剂然后在设置于管路L16中的膨胀阀54中膨胀，并部分闪蒸。
已经通过所述膨胀阀54的所述混合制冷剂已冷却到低于甲烷的沸点的温度(在这种情况下大约-167摄氏度)，并且从位于所述冷区Z3的上部的喷头55向下排出(或以与所述液化单元21中的所述原料气体相反的方向流动)。从所述喷头55喷出的所述混合制冷剂向下流动，同时与由设置在冷区Z3的所述管道系统32和53形成的上部管束进行热交换，并在与位于下方的所述喷头45喷出的所述混合制冷剂混合后向下流动，向下流动的同时与由位于中间区Z2的所述管道系统31，43和52所形成的中间管束以及由位于暖区Z1的所述管道系统22a,22b,30,42a,42b,51a和51b形成的下部管束进行热交换。
从所述喷头45和55喷出的所述混合制冷剂最后经由连接到所述液化单元21的底端的管路L17作为低压(LP)混合制冷剂(MP)气体排出。设置于所述液化单元21中的用于所述混合制冷剂的设备(如制冷剂分离器41)形成本身已知的用于所述混合制冷剂的制冷循环的一部分，且输出到管路L17的所述混合制冷剂在通过所述压缩机和所述冷凝器后经由管路L12被再循环到制冷剂分离器41。
如上所述，引入所述液化系统1中的所述原料气体在所述膨胀步骤，所述冷却步骤，所述蒸馏步骤，所述压缩步骤以及所述液化步骤中被处理之后被有效地液化。这种液化系统可应用于，例如，用于产生液化天然气(LNG)的基本负荷液化厂(baseloadliquefactionplant)，所述液化天然气(LNG)主要由从天然气田开采的所述原料气体的甲烷构成。
表1
No. (i) (ii) (iii) (iv) (v) (vi) (vii) (viii) (ix)
气相分数 1.00 1.00 1.00 0.00 0.93 0.00 1.00 1.00 0.00
温度[℃] 20.08 8.32 -42.58 177.19 -65.24 -65.24 -65.24 -50.99 -161.55
压力[kPa] 5830.00 4850.00 4700.00 4705.00 4400.00 4400.00 4400.00 5483.00 120.00
摩尔流速[kgmole/h] 42000 42000 45020 313 45020 3334 41686 41686 41700
质量流速[kg/h] 719619 719619 783504 19764 783504 83548 699948 699948 698733
摩尔分数
氮气 0.008199590 0.000033626 0.008260844
甲烷 0.949952502 0.043508871 0.956667221
乙烷 0.024998750 0.032339550 0.024931118
丙烷 0.009999500 0.143654595 0.009076200
丁烷 0.001999900 0.165149865 0.000793571
正丁烷 0.001999900 0.232835468 0.000268518
异戊烷 0.000499975 0.066891831 0.000001710
正戊烷 0.000499975 0.067093928 0.000000817
正己烷 0.000599970 0.080591893 0.000000000
苯 0.000499975 0.067159786 0.000000000
甲苯 0.000099995 0.013432078 0.000000000
对二甲苯 0.000049998 0.006716040 0.000000000
正庚烷 0.000499975 0.067160391 0.000000000
正辛烷 0.000099995 0.013432079 0.000000000
(第一和第二对比例)
图2和3是示出作为本发明的第一实施例的第一和第二个比较例给出的、天然气液化的常规系统中液化过程流程的示意图。在常规的天然气的液化系统101和201中，对应于所述第一实施例的液化系统的部件相对应的部件标以相同的标号。表2和3分别示出第一和第二比较例的所述液化系统中的所述原料气体的温度，压力，流速和摩尔分数。应当指出的是，第二比较例的所述液化系统201基于在专利文献1(US4，065，278)中公开的现有技术。
如图2中所示，所述第一比较例的所述液化系统101没有设有在第一实施例的液化系统1中使用的所述第一膨胀机3和第一压缩机4，从所述除水单元2排出的所述原料气体经由管路L101转递到冷却器110。冷却器单元通过将冷却器11和冷却器12串联连接所述冷却器110的下游端而形成，从而使得所述原料气体通过在三个冷却器110，11和12中进行热交换而依次冷却，所述冷却器110，11和12分别使用高压(HP)、中压(MP)和低压(LP)丙烷制冷剂。从所述下游端的所述冷却器12排出的所述原料气体具有约-34.5摄氏度的温度和约5,680kPaA的压力。所述原料气体随后通过在管路L4中的膨胀阀113中膨胀而减压，然后被引入所述蒸馏单元15。
在所述液化系统101中，形成在所述第一气液分离容器23中的气相组分的和基本上由甲烷构成的所述原料气体经由管路L102被引入位于所述液化单元21的中间区Z2的所述管道系统31中。从所述第一气液分离容器23输出到管路L12的所述原料气体具有约-65.3摄氏度的温度和约kPaA的压力。
表2
No. (i) (ii) (iii) (iv) (v) (vi) (vii) (viii)
气相分数 1.00 0.99 1.00 0.00 0.93 0.00 1.00 0.00
温度[℃] 20.08 -34.50 -42.58 176.73 -65.25 -65.25 -65.25 -161.56
压力[kPa] 5830.00 5680.00 4700.00 4705.00 4400.00 4400.00 4400.00 120.00
摩尔流速[kgmole/h] 42000 42000 45020 314 45020 3334 41686 41700
质量流速[kg/h] 719619 719619 783488 19624 783454 83495 699951 696348
摩尔分数
氮气 0.008199590 0.000072318 0.008260784
甲烷 0.949952502 0.064051796 0.956622861
乙烷 0.024998750 0.031841875 0.024947225
丙烷 0.009999500 0.129428030 0.009100267
丁烷 0.001999900 0.161816482 0.000796567
正丁烷 0.001999900 0.231738008 0.000270095
异戊烷 0.000499975 0.066667173 0.000001771
正戊烷 0.000499975 0.066846201 0.000000423
正己烷 0.000599970 0.080282498 0.000000003
苯 0.000499975 0.066901980 0.000000003
甲苯 0.000099995 0.013380485 0.000000000
对二甲苯 0.000049998 0.006690243 0000000000
正庚烷 0.000499975 0.066902427 0.000000000
正辛烷 0.000099995 0.013380486 0.000000000
如在图3中所示，第二比较例的所述液化系统201是第一比较例的液化系统101的改进，并设置有第一膨胀机3和第一压缩机4。然而，与在第一实施例的液化系统1中使用的第一膨胀机3相反，所述膨胀机3被位于所述冷却单元的下游侧(在这种情况下所述冷却单元由三个冷却器110，11和12构成)。在所述液化系统201中，从所述冷却器12排出的所述原料气体被转递到分离器213，以被分离成气体组分和液体组分。在所述分离器213中形成所述气相组分的所述原料气体被转递到所述膨胀机3，将在其内膨胀，然后经由管路L204被转递到所述蒸馏单元15。在所述分离器213中形成液体组分的所述原料气体的部分被输出到设有膨胀阀214的管路L205。已在所述膨胀阀214被膨胀的液体然后经由管路L204与来自所述膨胀机3的所述原料气体一起被转递到所述蒸馏单元15。
就所述蒸馏单元15的下游的部分而言，所述液化系统201类似于第一实施例中的所述液化系统201，已被所述压缩机4输出到管路L10的所述原料气体具有大约-54.7摄氏度的温度和大约kPaA的压力。
表3
No. (i) (ii) (iii) (iv) (v) (vi) (vii) (viii) (ix)
气相分数 1.00 1.00 1.00 0.00 0.94 0.00 1.00 1.00 0.00
温度[℃] 20.08 -45.36 -44.83 208.13 -64.56 -64.56 -64.56 -54.74 -161.59
压力[kPa] 5830.00 4705.00 4700.00 4705.00 4400.00 4400.00 4400.00 5120.00 120.00
摩尔流速[kgmole/h] 42000 41783 44200 302 44200 2500 41700 41700 41700
质量流速[kg/h] 719619 709009 764342 19107 764342 63861 700471 700471 694674
摩尔分数
氮气 0.008199590 0.000051871 0.008259333
甲烷 0.949952502 0.053398407 0.956509212
乙烷 0.024998750 0.032075932 0.024927984
丙烷 0.009999500 0.133750785 0.009066826
丁烷 0.001999900 0.153843084 0.000893180
正丁烷 0.001999900 0.230805233 0.000340430
异戊烷 0.000499975 0.069219794 0.000002448
正戊烷 0.000499975 0.069480324 0.000000589
正己烷 0.000599970 0.083472642 0.000000000
苯 0.000499975 0.069560398 0.000000000
甲苯 0.000099995 0.013912204 0.000000000
对二甲苯 0.000049998 0.006956102 0.000000000
正庚烷 0.000499975 0.069561020 0.000000000
正辛烷 0.000099995 0.013912205 0.000000000
通过比较本发明与第一和第二比较例可以理解的是，根据本发明的液化系统1能够使得通过膨胀更高温度和更高压力的原料气体产生更大的动力，因为相比于具有位于所述冷却单元110,112的下游侧的所述膨胀机3的第二比较例的所述液化系统201，所述第一膨胀机3位于第一冷却单元11，12的上游侧。因此，可以以增加的动力驱动所述第一压缩机4(或可以增加所述第一压缩机4的所述出口压力)，从而能够增加引入所述液化单元21的原料气体的压力，并有利地增加在液化单元21中的液化过程的效率。
所说明的实施例的所述液化系统1提供一个额外的优势在于减少所述冷却单元所需的冷却容量(从而省略第二个比较例中的冷却器110)，因为由于所述第一膨胀机3位于所述第一冷却单元11，12的上游侧，所述原料气体的温度通过所述第一膨胀机3中所述原料气体的膨胀被降低。在所说明的实施例中的所述液化系统1中，可以省略放置于所述冷却单元和所述膨胀机3之间的用于去除所述原料气体的冷凝物的气液分离容器(分离器213)。
(第一实施例的第一、第二和第三变形例)
图4，5和6为示出作为第一实施例的第一、第二和第三变形例分别给出的所述天然气液化系统中的液化处理流程的示意图。在图4，5和6中所示的液化系统中，对于对应于第一实施例(以及其它变形例)的液化系统1的那些部件的部件标以相同数字，除了下面将讨论的内容外，这些部件将在以下讨论中省略其说明。
如图4中所示，所述第一变形例的所述液化系统1中，所述热交换器69被设置在管路L4和管路L9之间。因此，在被引入第一压缩机4之前，在所述第一气液分离容器23中分离为所述气相组分并流过所述管路L9的所述原料气体通过与经由管路L4从所述冷却单元12流至所述蒸馏单元15的所述原料气体进行热交换来加热。由所述第一压缩机4压缩的所述原料气体经所述管路L10引入所述液化单元21。所述管路L10的下游端被连接到位于暖区Z1的管道系统30，所述暖区Z1呈现所述液化单元21的最高温度。所述管道系统30与管道系统22，管道系统42以及管道系统51一起形成位于暖区Z1的管束，其中所述蒸馏单元15的顶部馏分被引入所述管道系统22，混合制冷剂流过所述管道系统42和管道系统51。
由于这种设置，在所述第一实施例的第一变形例中，即使当经由管路L10被引入所述液化单元21的所述原料气体的温度水平应低于适当的范围，所述原料气体的温度能够通过在所述热交换器69中进行热交换而被升高至适当的水平。换句话说，在所述第一实施例的第一变形例中，在压缩后管路L10中的所述原料气体的温度能够接近所述液化单元21中的引入点(管道系统30)处的温度(优选地偏差低于10摄氏度)，从而能够减小所述液化单元21的热负荷(或最小化热应力的产生)。
只要所述管路L10中的所述原料气体的温度在压缩后能够与所述液化单元21的引入点处的温度接近，在第一变形例中的热交换器69的设置能够自由改变。例如，在图5中所示的第二变形例的所述液化系统1中，所述热交换器69设置在管路L4和管路L10之间。由所述第一压缩机4压缩并流过所述管路L10的所述原料气体，在被引入所述液化单元21之前，通过与流过管路L4的所述原料气体进行热交换而冷却。在第二变形例中，因为由所述热交换器69加热的所述原料气体没有受到如第一压缩机4的装置的介入，而被引入所述液化单元21，所述被引入所述液化单元1的所述原料气体的温度可以容易地控制。
如图6中所示，所述第三变形例的所述液化系统中，所述热交换器69被设置在管路L4和管路L6之间。因此，从所述蒸馏单元15分离为顶部馏分并流过所述管路L6的所述原料气体，在被引入所述液化单元21(所述管道系统22)之前，通过与流过管路L4的所述原料气体进行热交换而加热。特别地，在所述第三变形例中，即使当所述原料气体由含有如表1所示的相对较低水平的较重组分(高碳烃类)的天然气(贫气)构成，在所述蒸馏步骤之后流过所述管路L6的所述原料气体的温度可能低于适当的范围时，能够通过在热交换器69中进行热交换使得所述原料气体的温度升高到适当的水平。
(第一实施例的第四变形例)
图7为示出作为第一实施例的第四变形例给出的天然气液化系统中的液化处理流程的示意图。在图7中所示的液化系统中，对于对应于第一实施例(包括其变形例)的液化系统1的那些部件的部件标以相同数字，除了下面将讨论的内容外，这些部件将在以下讨论中省略其说明。
第四变形例类似于第三变形例，但进一步包括设置于所述管路L9和所述管路L10之间的热交换器79。在管路L10中进一步设置有使用低压(LP)丙烷制冷剂(C3R)的冷却器80。因此，从所述第一压缩机4排出的所述原料气体，在被引入所述液化单元21之前，通过与流过管路L9的所述原料气体进行热交换而冷却。所述管路L10的下游端被连接到位于中间区Z2的管道系统31。
在第四变形例中，从所述第一压缩机4排出的所述原料气体能够被引入中间区Z2中。因此，暖区Z1中的管束能够由三个所述管道系统22、42和51形成，而在中间区Z2的管束能够由三个所述管道系统31、43和52形成。因此，在第四变形例中，当所述液化单元21通过使用线轴缠绕式热交换器形成时，相比所述第三变形例的设置，在暖区Z1和中间区Z2的所述管道系统的设置可以被优化(通过在不同区之间均匀分布所述管道系统)，从而防止所述液化单元21的尺寸变得过大。类似于在所说明的实施例中的第一和第二冷却器11和12，第五冷却器80使用丙烷制冷剂，也可以使用其他形式的气冷器或水冷器。
(第一实施例的第五变形例)
图10为示出作为本发明的第一实施例的第五变形例给出的天然气液化系统中的液化处理流程的示意图。在图10中所示的液化系统中，对于对应于第一实施例(包括其变形例)的液化系统1的那些部件的部件标以相同数字，除了下面将讨论的内容外，这些部件将在以下讨论中省略其说明。
第五变形例类似于上面所讨论的第四变形例，但省略了在所述第四变形例的所述第五冷却器80，并且在由所述蒸馏单元15开始的所述管路L6和由所述第一压缩机4开始的所述管路L10之间添加所述热交换器100。其结果是，代替由第五冷却器80冷却，从所述第一压缩机4排到管路L10的所述原料气体通过从所述蒸馏装置15排到所述管路L6的原料气体(顶部馏分)冷却，且与第四变形例类似地被引入热交换器79。同时，从所述蒸馏单元15排出的所述原料气体在所述热交换之后通过管路L6被引入所述液化单元21，并且随后通过所述管道系统22冷却。由于这样的设置，在第五变形例中，所述原料气体由所述第五冷却器80的冷却如同在第四实施例中，可以通过在所述热交换器100的热交换增加或取代。在第八实施例中，省略在第五实施例中所使用的热交换器69，但也可以设置热交换器69，以使得从所述蒸馏单元15排到管路L6的所述原料气体经由热交换器69被引入到热交换器100。
(第二实施例)
图8为示出作为本发明的第二实施例给出的所述天然气液化系统中的液化处理流程的示意图。在图8中所示的液化系统中，对于对应于第一实施例的液化系统1的那些部件的部件标以相同数字，除了下面将讨论的内容外，这些部件将在以下讨论中省略其说明。
在所述第二实施例的液化系统1中，含有88mol％甲烷的富气用作所述原料气体。在此液化系统中，在所述蒸馏单元15被分离成顶部馏分的所述原料气体经由管路L19直接引入到所述第一压缩机4从而被压缩。所述原料气体随后在暖区Z1中的管道系统22中预冷却，并经由管路L21转递给第一气液分离容器23。
所述第一气液分离容器23分离所述原料气体的液相组分(冷凝物)，并且构成所述液相组分的液态烃类通过设置于管路L22的膨胀阀89再循环到所述蒸馏单元15。同时，主要由甲烷构成并在第一气液分离容器23中形成液相组分的所述原料气体经由管路L23被转递到所述液化单元21中的所述管道系统31。
在所述第二实施例的液化系统1中，因为第一气液分离容器23设置在第一压缩机4的下游侧，以及从所述第一压缩机4排出的原料气体经由位于暖区Z1中的管道系统22被引入第一气液分离容器23中，能够使得所述原料气体的温度接近所述液化单元21的所述暖区Z1的温度水平。此外，由于所述原料气体在所述液化单元21的暖区Z1(管道系统22)中冷却，并且从第一气液分离容器23排出的所述气相组分被引入中间区Z2(管道系统31)，能够容易地使得所述原料气体的温度接近所述液化单元21的中间区Z2的温度水平。另外，因为从所述第一气液分离容器23排出的所述原料气体可通过第一压缩机4被压力输送，能够省略在一些包括第一实施例的实施例中设置于所述再循环管路(管路L21)的再循环泵24，所述再循环管路从第一气液分离容器23延伸至所述蒸馏单元15。
在所述液化单元21的所述原料气体的液化中，提高所述压缩机4的出口压力(或增加被引入所述液化单元21的所述原料气体的压力)是有利的。然而，正如在第一实施例的情况下，当在所述第一气液分离容器23中被分离的所述蒸馏单元15的顶部馏分在所述液化单元21中被冷却，以及所述分离的气相组分在被引入到所述液化单元21之前由所述第一压缩机4压缩时，因为所述原料气体的温度通过在所述液化单元21之前的所述第一压缩机4增大，所述温度取决于所述原料气体的组分、压力以及进料速度，所述原料气体的温度水平可能偏离用于引入所述液化单元21的合适的范围，从而使所述液化单元21上的热负荷可能变得过量。这样的问题可以通过改变将所述原料气体引入液化单元21的点来解决，但是，当主热交换器由一种不允许引入点被轻易改变的诸如线轴缠绕式热交换器构成时，情况就不一定如此了。因此，如果在蒸馏单元15中分离为顶部馏分的原料气体经由管路L19直接转发到第一压缩机4被压缩，由第一压缩机4压缩的原料气体在液化单元21中的暖区Z1冷却，经冷却的原料气体在第一气液分离器23分离，将原料气体中的被分离的气相组分被引入液化单元21的中间区域Z2(暖区Z1的下游)中，于本实施例的情况下，材料气体的温度可在适当的范围内保持(或原料气体的温度可以接近于在液化单元21的引入点的温度水平)。
(第二实施例的第一变形例)
图9为示出作为本发明第二实施例的第一变形例给出的所述天然气液化系统中的液化处理流程的示意图。在图9中所示的液化系统中，对于对应于第二实施例的液化系统1的那些部件的部件标以相同数字，除了下面将讨论的内容外，这些部件将在以下讨论中省略其说明。
如图9所示，第一变形例的液化系统1包括位于所述管路L4和管路L20之间的热交换器69，从而使得从第一压缩机4排出并通过管路L20引导的原料气体通过与流经管路L4的原料气体进行热交换而被加热，然后被引入到位于液化单元21的暖区Z1的管道系统。在所述第二实施例的第一变形例中，在所述热交换器69中加热的所述原料气体没有受到第一压缩机4的介入，而被直接引入所述液化单元21，因此所述被引入所述液化单元21的所述原料气体的温度可以容易地控制。
只要压缩后所述管路L20中的所述原料气体的温度能够与所述液化单元21的引入点处的温度接近，在第二实施例中的第一变形例中的热交换器69的定位在不偏离本发明的精神下，能够发生各种改变。
本发明已由具体实施方式描述，但这些实施例只是例子，并不以任何形式限制本发明。根据本发明的用于天然气液化的所述液化系统和液化方法的各种组件并不一定完全不可或缺，但可以不脱离本发明的精神下被适当地取代和省略。

Claims (34)

1.用于冷却天然气进料的方法，包括：
a)减少天然气进料的压力，以产生减压的原料气体；
b)从所述减压的原料气体中除去重质组分以产生顶部馏分和底部馏分；
c)冷却所述顶部馏分以产生冷却的顶部馏分；
d)将所述冷却的顶部馏分分离成气相组分和液相组分；
e)增加气相组分的压力以产生压缩的原料气体；以及
f)在所述气相组分和所述压缩的原料气体之间进行热交换，以至少产生冷却的压缩的原料气体。
2.根据权利要求1所述的方法，还包括在步骤(b)中去除重质组分之前冷却步骤(a)的所述减压的原料气体。
3.根据权利要求1所述的方法，还包括至少部分液化步骤(f)的所述冷却的压缩的原料气体。
4.根据权利要求1所述的方法，还包括在步骤(f)之前冷却步骤(e)的所述压缩的原料气体。
5.根据权利要求1所述的方法，其中在步骤(c)中通过将所述顶部馏分引入线轴卷绕式热交换器的温暖区域中来冷却所述顶部馏分。
6.根据权利要求5所述的方法，其中通过将所述冷却的压缩的原料气体引入所述线轴卷绕式热交换器的中间区域来进一步冷却步骤(f)的所述冷却的压缩的原料气体。
7.根据权利要求1所述的方法，其中步骤(b)中所述重质组分的除去在蒸馏单元中进行。
8.根据权利要求1所述的方法，还包括将步骤(d)的所述液相组分再循环至所述蒸馏单元。
9.根据权利要求1的方法，还包括在步骤(c)之前在步骤(b)的顶部馏分和所述减压的原料气体之间进行热交换。
10.根据权利要求1的方法，其中步骤(f)包括在步骤(d)的所述气相组分，步骤(e)的所述压缩的原料气体和步骤(a)的所述减压的原料气体之间进行热交换。
11.用于冷却天然气进给的方法，包括：
a)减少天然气进料的压力，以产生减压的原料气体；
b)从所述减压的原料气体中除去重质组分以产生顶部馏分和底部馏分；
c)在所述减压的原料气体和所述顶部馏分之间进行热交换，以至少产生发生热交换的顶部馏分；
d)冷却所述发生热交换的顶部馏分以产生冷却的顶部馏分；
e)将所述冷却的顶部馏分分离成气相组分和液相组分；
f)增加气相组分的压力以产生压缩的原料气体；以及
g)冷却所述压缩的原料气体。
12.根据权利要求11所述的方法，还包括在步骤(b)中去除重质组分之前冷却步骤(a)的所述减压的原料气体。
13.根据权利要求11所述的方法，其中在步骤(g)中通过将所述压缩的原料气体引入一个或多个热交换器来冷却所述压缩的原料气体。
14.根据权利要求11所述的方法，其中步骤(b)中所述重质组分的除去在蒸馏单元中进行。
15.根据权利要求14所述的方法，还包括将步骤(e)的所述液相组分再循环至所述蒸馏单元。
16.用于冷却天然气进给的方法，包括：
a)减少天然气进料的压力，以产生减压的原料气体；
b)从所述减压的原料气体中除去重质组分以产生顶部馏分和底部馏分；
c)冷却所述顶部馏分以产生冷却的顶部馏分；
d)将所述冷却的顶部馏分分离成气相组分和液相组分；
e)增加气相组分的压力以产生压缩的原料气体；以及
f)在步骤a)中产生的所述减压的原料气体和所述压缩的原料气体之间进行热交换，以至少产生发生热交换的压缩的原料气体。
17.根据权利要求16所述的方法，还包括在步骤(f)中的热交换之前冷却步骤(a)的所述减压的原料气体。
18.用于冷却天然气进给的方法，包括：
a)减少天然气进料的压力，以产生减压的原料气体；
b)在所述蒸馏单元中从所述减压的原料气体除去重质组分以产生顶部馏分和底部馏分；
c)冷却并部分液化所述顶部馏分以产生冷却的顶部馏分；
d)分离所述冷却的顶部馏分以生成气相组分和液相组分；
e)将所述液相组分再循环至所述蒸馏单元；
f)在所述减压的原料气体和所述气相组分之间进行热交换，以至少产生发生热交换的气相组分；以及
g)增加所述发生热交换的气相组分的压力以产生压缩的原料气体。
19.根据权利要求18所述的方法，还包括在步骤(f)中的热交换之前冷却步骤(a)的所述减压的原料气体。
20.用于冷却天然气进给的方法，包括：
a)减少天然气进料的压力，以产生减压的原料气体；
b)从所述减压的原料气体中除去重质组分以产生顶部馏分和底部馏分；
c)增加所述顶部馏分的压力以产生压缩的原料气体；以及
d)在所述顶部馏分和所述压缩的原料气体之间进行热交换，以至少产生冷却的压缩的原料气体。
21.根据权利要求20所述的方法，还包括在步骤(b)之前冷却步骤(a)的所述减压的原料气体。
22.根据权利要求20所述的方法，还包括在步骤(d)中的热交换之前冷却步骤(c)的所述压缩的原料气体。
23.用于液化天然气进料的系统，包括：
第一膨胀机，其减少所述天然气进料的压力来产生减压的原料气体；
蒸馏单元，其用于从所述减压的原料气体中除去重质组分来产生顶部馏分和底部馏分；
第一热交换器，其用于冷却所述顶部馏分来产生冷却的顶部馏分；
第一气液分离容器，其将所述冷却的顶部馏分分离为气相组分和液相组分；
第一压缩机，其用于压缩所述气相组分以产生压缩的原料气体；以及
第二热交换器，其用于在所述气相组分和所述压缩的原料气体之间进行热交换。
24.根据权利要求23所述的系统，还包括用于在引入所述蒸馏单元之前冷却所述减压的原料气体的第一冷却单元。
25.根据权利要求23所述的系统，还包括用于在引入所述第二热交换器之前冷却所述减压的原料气体的第二冷却单元。
26.根据权利要求23所述的系统，其中所述第一热交换器是线轴卷绕式热交换器的温暖区域。
27.根据权利要求26所述的系统，其中还包括第三热交换器，其用于在所述压缩的原料气体通过第二热交换器之后冷却所述压缩的原料气体，其中所述第三热交换器是所述线轴卷绕式热交换器的中间区域。
28.根据权利要求23所述的系统，还包括管道，其将所述液相组分从所述第一气液分离容器作为回流再循环至所述蒸馏单元。
29.根据权利要求23所述的系统，进一步包括第四热交换器，其用于对来自所述蒸馏单元的所述顶部馏分和所述减压的原料气体之间进行热交换。
30.根据权利要求23的系统，其中所述第二热交换器在所述气相组分、所述压缩的原料气体和所述减压的原料气体之间进行热交换。
31.根据权利要求23所述的系统，其中所述第一膨胀机生产动力，以及所述第一压缩机使用由第一膨胀机生成的动力。
32.用于液化天然气进料的系统，包括：
第一膨胀机，其减少所述天然气进料的压力来产生减压的原料气体；
蒸馏单元，其用于从所述减压的原料气体中除去重质组分来产生顶部馏分和底部馏分；
第一热交换器，其用于在所述顶部馏分和所述减压的原料气体之间进行热交换，以至少产生发生热交换的顶部馏分。
第二热交换器，其用于冷却所述发生热交换的顶部馏分来产生冷却的顶部馏分；
第一气液分离容器，其将所述冷却的顶部馏分分离为气相组分和液相组分；以及
第一压缩机，其用于压缩所述气相组分以产生压缩的原料气体。
33.根据权利要求32所述的系统，还包括用于在引入所述蒸馏单元之前冷却所述减压的原料气体的第一冷却单元。
34.用于液化天然气进料的系统，包括：
第一膨胀机，其减少所述天然气进料的压力来产生减压的原料气体；
第一冷却单元，其用于冷却所述减压的原料气体以产生冷却的减压的原料气体；
蒸馏单元，其用于从所述冷却的减压的原料气体中除去重质组分来产生顶部馏分和底部馏分；
线轴卷绕式热交换器的温暖区域，其用于冷却所述顶部馏分来产生冷却的顶部馏分；
第一气液分离容器，其将所述冷却的顶部馏分分离为气相组分和液相组分；
管道系统，其将所述液相组分再循环至所述蒸馏单元；
第一压缩机，其用于压缩所述气相组分以产生压缩的原料气体；
第二冷却单元，其用于冷却所述压缩的原料气体以产生冷却的压缩的原料气体；
第三热交换器，其用于在所述冷却的压缩的原料气体和所述气相组分之间进行热交换，以产生另外的冷却的压缩的原料气体；以及
所述线轴卷绕式热交换器的中间区域，其用于至少部分液化所述另外的冷却的压缩的原料气体。
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