CN1813046A - 同时生产可液化天然气和天然气液体的馏分的方法和装置 - Google Patents

同时生产可液化天然气和天然气液体的馏分的方法和装置 Download PDF

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CN1813046A
CN1813046A CNA2004800183558A CN200480018355A CN1813046A CN 1813046 A CN1813046 A CN 1813046A CN A2004800183558 A CNA2004800183558 A CN A2004800183558A CN 200480018355 A CN200480018355 A CN 200480018355A CN 1813046 A CN1813046 A CN 1813046A
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natural gas
sweet natural
tower
liquefiable
king
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CN100588702C (zh
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H·帕拉多斯柯
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Technip Energies France SAS
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Technip France SAS
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    • 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
    • F25J3/0228—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 separated product stream
    • F25J3/0238—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 separated product stream separation of CnHm with 2 carbon atoms or more
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    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
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Abstract

本发明的方法包括下述步骤：(a)将原料天然气(103)引入到第一蒸馏塔(31)内，所述第一蒸馏塔(31)产生预处理的天然气(111)作为顶部产物，所述预处理的天然气(111)基本上不含C6 +烃；(b)将预处理的天然气(111)引入到含至少一个第二蒸馏塔(49)的NGL回收单元(19)中，以便一方面产生纯化的天然气(151)作为塔顶产物，并且另一方面产生NGL馏分(15)；和(c)由来自步骤(b)的纯化的天然气(151)形成所述可液化天然气(161)。

Description

同时生产可液化天然气和天然气液体的馏分的方法和装置
本发明涉及一种由含有氮气、甲烷、C2-C5烃和C6 +重质烃的原料天然气同时生产可液化天然气和天然气液体(NGL)的馏分的方法，这类方法包括下述步骤：
(a)预处理所述原料天然气，以获得预处理的天然气；
(b)将来自步骤(a)的预处理的天然气冷却到接近于其露点的温度；
(c)使来自步骤(b)的冷却的预处理的天然气膨胀，并且膨胀的天然气被引入到含至少一个主蒸馏塔的NGL回收单元中，以便一方面产生作为塔顶产物的纯化的天然气，并且另一方面产生所述的NGL馏分；和
(d)由来自步骤(c)的纯化的天然气形成所述可液化天然气。
本发明的方法适合于用于由从地下提取的天然气生产液化天然气(将被称为“LNG”)作为主产物和天然气液体(将被称为“NGL”)的馏分作为副产物的装置。
在本发明中，NGL要理解为是指可从天然气中提取的C2 +到C3 +烃。作为实例，这些NGL可包括乙烷、丙烷、丁烷和C5 +烃。
与没有提取NGL生产的LNG相比，在提取NGL之后生产的LNG具有较低的热值。
已知的天然气液化装置依次包括用于生产可液化气体的单元、用于实际液化的单元、和从LNG中除氮的单元。用于生产可液化气体的单元必须包括用于除去在液化过程中可结晶的C6 +重质烃的设备。
为了同时生产可液化天然气和NGL，可使用例如前述类型的方法，例如在申请FR-A-2817766中所述的方法。
这种方法具有对于室温下生产天然气和对于NGL提取来说优化的热力学效率。
因此，如果所得天然气必须液化的话，则该方法并不完全令人满意。这是因为液化所得天然气所需的能量消耗相对较高。
本发明的主要目的是弥补这一缺点，也就是说，本发明提供一种用于同时生产LNG和NGL馏分的方法，该方法比已有的方法更加经济且更加灵活。
为此，本发明的目的是一种前述类型的方法，其特征在于步骤(a)包括下述子步骤：
(a1)将原料天然气冷却到接近其露点的温度；
(a2)来自步骤(a1)的所述冷却的原料天然气被引入到辅助蒸馏塔中，所述辅助蒸馏塔产生作为顶部产物的所述预处理的天然气，该预处理的天然气基本上不含C6 +烃，这个第一辅助蒸馏塔此外还产生基本上C6 +重质烃的馏分。
本发明的方法可包括单独或者任何可能的组合形式的一个或多个下述特征，
-步骤(d)包括下述子步骤：
(d1)在至少第一压缩机中，在液化压力下压缩从所述主塔的顶部提取的纯化的天然气；
(d2)在第一换热器中，通过与从主塔顶部提取的所述纯化的天然气进行热交换，来自步骤(d1)的压缩的纯化天然气被冷却，以便生产可液化的天然气；
-步骤(b)包括下述子步骤：
(b1)通过在第二换热器中与从第二主塔中提取的纯化天然气进行热交换，来自步骤(a)的预处理的天然气被冷却；
-步骤(c)包括下述子步骤：
(c1)将来自步骤(b)的冷却的预处理天然气引入到分离鼓中，以获得液体流和气体流；
(c2)来自步骤(c1)的气体流在连接到第一压缩机上的涡轮机中膨胀；
(c3)将来自步骤(c2)的流在中间高度N3处引入到主塔内；
(c4)使来自步骤(c1)的液体流膨胀，并将这一膨胀的液体流在高度N 3下方的高度N2处引入到主塔内；
-在步骤(d1)中，通过第一压缩机输出的压缩的纯化天然气在通过外部能源供应的第二压缩机内压缩，以便达到所述的液化压力；
-主蒸馏塔的压力大于35巴；
-可液化天然气进一步包括直接来自步骤(a)的一部分预处理的天然气；
-该方法包括启动阶段，其中可液化天然气主要或完全由直接来自步骤(a)的预处理的天然气组成，所述可液化天然气相对富含C2-C5烃，并且该方法包括随后的生产阶段，其中根据可液化天然气中所需的C2-C5烃含量来调节可液化天然气中直接来自步骤(a)的预处理天然气的部分；和
-通过辅助塔生产的液体被膨胀并被引入到主塔中。
本发明的主题还在于一种用于由含有氮气、甲烷、C2-C5烃和C6 +重质烃的原料天然气同时生产可液化天然气和天然气液体(NGL)馏分的装置，这类装置包括：
(a)用于预处理所述原料天然气以获得预处理的天然气的单元；
(b)用于将预处理的天然气冷却到接近其露点的温度的设备；
(c)用于回收NGL的单元，其包括使冷却的预处理的天然气膨胀的设备，并且包括至少一个主蒸馏塔，所述主蒸馏塔一方面生产作为塔顶产物的纯化的天然气，并且另一方面生产所述的NGL馏分；和
(d)用于将来自步骤(c)的纯化的天然气传送到可液化天然气管线中的设备；
其特征在于该预处理单元包括：
(a1)用于将原料天然气冷却到接近其露点的温度的设备；
(a2)用于蒸馏冷却的原料天然气的辅助蒸馏塔，所述辅助蒸馏塔产生所述预处理的天然气作为顶部产物，它基本上不含C6 +馏分，这个辅助塔此外还产生基本上C6 +重质烃的馏分。
本发明的装置可包括单独或者任何可能的组合形式的一种或多种下述特征：
-用于形成可液化天然气的设备包括：
(d1)用于在液化压力下压缩从主塔顶部提取的纯化天然气的设备，它包括至少第一压缩机；
(d2)第一换热器，所述第一换热器使来自所述压缩设备的压缩纯化的天然气与从主塔顶部提取的所述纯化的天然气产生换热的关系，所述压缩的纯化天然气在这个第一换热器内冷却，为的是产生可液化天然气；
-用于冷却预处理天然气的设备包括第二换热器，所述第二换热器使这种气体与从主塔中提取的所述纯化的天然气产生换热的关系；
-用于回收NGL的单元包括：
(c1)用于分离冷却的预处理的天然气的分离鼓，所述鼓产生液体流和气体流；
(c2)用于使所述气体流膨胀的第一膨胀涡轮机，所述涡轮机连接到所述第一压缩机上；
(c3)用于在中间高度N3处将膨胀的气体流引入到主塔内的设备；
(c4)用于使所述液体流膨胀的设备和用于在N3下方的高度N2处将膨胀的液体流引入到主塔内的设备；
-用于压缩从主塔顶部提取的纯化天然气的设备此外包括通过外部能源驱动的第二压缩机，所述第二压缩机旨在将压缩纯化的天然气的压力增加到液化压力；和
-用于形成纯化的天然气的设备包括用于将直接来自预处理单元的预处理天然气的可调节部分选择性地引入到可液化天然气管线内的设备。
现在将结合单幅附图描述如何实施本发明的实施例，该附图示出了阐述本发明装置操作的方框图。
该附图所示的装置涉及由脱碳酸气和脱硫的干燥原料天然气源11生产作为主产物的LNG13和作为副产物的NGL馏分15。这个装置包括用于除去C6 +重质烃的单元17，用于回收NGL的单元19和液化单元21。
在下文中，液体流和输送其的管线这二者都将用相同的参考标记表示，并且所讨论的压力为绝对压力。
用于除去重质烃的单元17依次包括在源11下游的第一、第二和第三冷却器25、27、29和配有塔顶冷凝器的第一蒸馏塔或者辅助蒸馏塔31。这个塔顶冷凝器包括在第一塔31的顶部和第一分离鼓33之间的在一侧上的第四冷却器35，和在另一侧上的回流泵37。
NGL回收单元19包括第一、第二和第三换热器41、43、45，第二分离鼓47，第二蒸馏塔或者主蒸馏塔49，连接到第一压缩机53上的第一涡轮机51、通过外部能源56驱动的第二压缩机55、第五冷却器57和NGL提取泵59。
天然气液化单元21包括通过制冷循环69冷却的第四和第五换热器65、67。
这个循环69包括具有三级73A、73B、73C的压缩机73，所述压缩机配有第一和第二中间冷却器75A和75B和后冷却器75C，串联的四个冷却器77A-77D，第三分离鼓79和第一与第二水轮机81和83。
以下将描述如何实施本发明方法的实施例。
脱碳酸气和脱硫的干燥原料天然气流101的起始摩尔组成含有3.90％的氮气、87.03％的甲烷、5.50％的乙烷、2.00％的丙烷、0.34％的异丁烷、0.54％的正丁烷、0.18％的异戊烷、0.15％的正戊烷、0.31％的C6烃、0.03％的C7烃和0.02％的C8烃。
这种气体101依次在第一、第二和第三冷却器25、27、29内冷却，以便形成冷却的原料天然气103。所述气体103然后被引入到蒸馏塔31内。
这个塔31产生作为底部产物的C6 +重质烃的馏分105。这一馏分105在膨胀阀106中膨胀，以便产生重质烃的膨胀流107，将其在低高度N1处引入到第二蒸馏塔49中。
此外，第一塔31产生预处理的气体流109作为顶部产物。在第四冷却器35中冷却所述流109并部分冷凝，然后引入到第一分离鼓33内，在此进行构成预处理的天然气111的气相和构成回流液体112的液相之间的分离，所述液体作为回流液通过回流泵37返回到纯化塔内。
预处理的气体流111的摩尔组成含有3.9783％的氮气、88.2036％甲烷、5.3622％的乙烷、1.7550％丙烷、0.2488％的异丁烷、0.3465％的正丁烷、0.0616％的异戊烷、0.0384％的正戊烷和0.0057％的C6烃。
从所述流111中已基本上除去C+ 6烃。
预处理的天然气流111然后分成供给NGL回收单元19的流113和供给气体液化单元21的流115。通过控制两个相应的控制阀114和116来选择这两个流之间的分流。
在第二换热器43内冷却引入到回收单元19的所述流113，以便得到冷却的预处理天然气的两相流117。所述流117引入到第二分离鼓47，所述分离鼓47产生蒸汽流119和液体流121。液体流121在膨胀阀123内膨胀，然后在高度N1上方的高度N2处引入到塔49内。
蒸汽流119被分成主要部份125和次要部份127。
主要部份125在涡轮机51内膨胀，以便得到膨胀的主要部份129，将所述膨胀的主要部份129在高度N2上方的高度N3处引入到塔49内。
次要部份127在第三换热器45内冷却，在膨胀阀131内膨胀，然后在高高度N4处引入到蒸馏塔49内。高度N4在高度N3之上。
塔49还配有中间再沸器141。在N2下方和N1上方的高度N1 a处从这个塔中提取再沸器流143。所述流在第二换热器43内加温并在高度N1 a和高度N1之间的高度N1 b处再引入到第二塔49内。
从蒸馏塔49的底部通过泵59提取NGL馏分15。此外，底部再沸器145安装在塔49上，以便调节NGL馏分15中C1烃相对于C2烃的摩尔比。这一比例优选小于0.02。
因此，所述NGL馏分15含有0.3688％甲烷、36.8810％乙烷、33.8344％丙烷、6.1957％异丁烷、9.9267％正丁烷、3.3354％异戊烷、2.7808％正戊烷、5.7498％C6烃、0.5564％C7烃和0.3710％C8烃。
乙烷、丙烷和C4 +烃的相应提取量是36.15％、91.21％和99.3％。因此，通过本发明方法的乙烷回收量大于30％。丙烷回收量大于80％和优选大于90％。C4 +烃回收量大于90％和优选大于95％。
纯化天然气流151从塔49中作为顶部产物提取。所述流151依次在换热器45、换热器43，然后在换热器41内加温。应当指出，对于操作NGL回收单元19来说，不需要外部的冷源。
来自换热器41的加温的气体流153然后依次在第一压缩机51内，然后在第二压缩机55内压缩，以便产生处于液化压力下的气体流155。
所述流155在第五冷却器57内，然后在第一换热器41内冷却，为的是得到冷却的纯化气体流157。将所述流157与供给气体液化单元的流115混合，所述流115从用于除去C6 +重质烃的单元17中提取。所述流157和所述流115具有基本上相同的温度和压力并形成可液化的天然气流161。
该可液化的天然气流161的摩尔组成含有4.1221％氮气、91.9686％甲烷、3.7118％乙烷、0.1858％丙烷、0.0063％异丁烷、0.0051％正丁烷和0.0003％C5 +烃。
然后将可液化天然气流161依次在第四和第五换热器65、67内冷却，以便产生LNG流13。这一LNG流13然后在单元165内进行氮气除去步骤。
通过制冷混合物流201提供在第四和第五换热器65、67内的制冷。在第四冷却器77D内部分液化的所述流201被引入到分离鼓71内并分离成蒸汽相201和液相203。
所述流201以及液相和蒸汽相203和205的摩尔组成如下所述：
  流201(％)   流203(％)   流205(％)
  N2   4.0   10.18   1.94
  C1   42.4   67.90   33.90
  C2   42.6   20.18   50.07
  C3   11.0   1.74   14.09
蒸汽相203在换热器65内液化，以便得到液体流，然后在第五换热器67内低温冷却，得到低温冷却的液体流207。
这一低温冷却的液体流207在第一水轮机81内膨胀，然后在膨胀阀208内膨胀，以便得到第一制冷剂流209。所述流209在换热器67内汽化并使得气体161液化。
液相205在换热器65内低温冷却得到低温冷却流，所述低温冷却流又在第二水轮机83内膨胀，然后在膨胀阀210内膨胀，以便得到第二制冷剂流211。将所述流209和211混合，得到合并流213，所述合并流213在换热器65内汽化。该汽化使得流161冷却并使制冷剂混合物流201的蒸汽相203冷凝。然后，在压缩机77内压缩混合物流213，以便得到压缩的混合物流215，其中在下表中给出了所述压缩机的特征。
  压缩机   73A   73B   73C
  吸入温度(℃)   -37.44   34   34
  排出温度(℃)   67.25   68.70   68.15
  吸入压力(巴)   3.65   18.30   29.70
  排出压力(巴)   18.70   30.00   47.61
  多变效率(％)   82   82   82
  功率(kW)   74109   24396   21882
这一压缩混合物流215然后依次在四个串联连接的冷却器81内冷却，为的是形成流201。
一方面冷却原料天然气的第一、第二、第三和第四冷却器25、27、29、35，以及另一方面冷却混合物流201的四个冷却器77A-77D，使用相同的丙烷制冷循环(未示出)。这一循环包括四个下述汽化阶段：6.7℃和7.92巴；0℃和4.76巴；-20℃和2.44巴；-36℃和1.30巴。
通过下表的实例给出在附图中所示操作的装置的温度、压力和流速的模型。
  流   温度(％)   压力(巴)   流速(kg/h)
  13   -148   58.9   809567
  15   78   43.2   123436
  101   23   62.0   933003
  103   -18   61.1   933003
  105   -18   61.1   49888
  107   -23   39.8   49888
  111   -34   60.8   883115
  113   -34   60.8   883115
  115   -   -   0
  117   -47   60.1   883115
  123   -59   39.8   36469
  129   -66   39.8   675718
  131   -86   39.8   178092
  143   -48   39.6   124894
  151   -76   39.5   809567
  153   32   38.8   809567
  155   74   61.5   809567
  157   -34.6   60.1   809567
  161   -34.6   60.1   809567
  201   -34   46.1   1510738
  207   -148   44.9   303816
  209   -154   4.2   303816
  211   -130   4.1   1206922
  213   -128   4.1   1510738
  215   34   47.6   1510738
正如该实施例所述，蒸馏塔31的压力优选介于45至65巴。在第二塔内的压力优选大于35巴。
因此可优化每个塔的操作，以便一方面有利于在塔31内提取C6 +烃，并且另一方面有利于在塔49内提取乙烷和丙烷。
此外，在高于55巴的压力下生产纯化的气体流157和供给气体液化单元115的流。
这一方法使得可实现下表所示的节能，在下表中比较了在不具有辅助塔31的现有技术的装置内和在本发明的装置内所消耗的功率。
更确切地，在现有技术的装置内，原料天然气流101被直接输送到NGL提取单元19内，并且利用丙烷循环的冷却器25、27、29和35还起到在液化压力155下预冷却气体流的作用，这与其中使用换热器41进行这一预冷却的本发明的装置不同。
  现有技术的工艺   本发明的工艺
  混合的制冷剂压缩机73(kW)   119460   120387
  丙烷制冷剂压缩机(未示出)(kW)   69700   72174
  处理的气体压缩机55(kW)   20650   14964
  总计(kW)   209810   207525
因此，本发明的装置使得可同时生产LNG13和NGL馏分15，且与现有技术的装置相比，节约2285kW。
此外，当启动本发明的装置时，来自用于除去重质烃的单元17的所有预处理的天然气流111经供料流115被直接输送到液化单元21内。因此，所产生的LNG具有相对高的热值。然后，在没有影响液化单元21产率的情况下，逐渐启动NGL回收单元19。然后通过用于NGL回收单元的供料流113和用于气体液化单元的115的相对流速来调节所产生的LNG的热值。
同样，在NGL回收单元19中出现问题的情况下，来自重质烃除去单元17的所有预处理的天然气流111经供料流115直接输送到液化单元21。
作为一种变通方案，NGL回收单元可包括安装在第二蒸馏塔下游且在比第二塔的压力高或者低的压力下操作的第三蒸馏塔。这个第三塔用于富集具有特定组分(例如丙烷)的NGL。在EP-A-0535752中公开了这一单元的实例。
由于以上所述的本发明，因此可得到以经济和灵活的方式同时生产LNG和NGL且C2-C5烃的提取量高的装置。令人惊奇地，通过在NGL回收单元上游插入辅助蒸馏塔并通过将来自这个塔的顶部产物部份引入到这个单元内，会显著降低能耗。
特别是在该装置的启动阶段期间或者在NGL回收单元出现故障的情况下，通过将这一顶部产物部份的至少一部分直接导入液化单元，从而增加了这一装置的产率。
此外，这一装置使得可生产可调节热值的LNG。

Claims (13)

1.一种用于由含有氮气、甲烷、C2-C5烃和C6 +重质烃的原料天然气(101)同时生产可液化天然气(161)和天然气液体(NGL)馏分(15)的方法，这类方法包括下述步骤：
(a)预处理所述原料天然气(101)，以获得预处理的天然气(111)；
(b)将来自步骤(a)的预处理的天然气(111)冷却到接近其露点的温度；
(c)使来自步骤(b)的冷却的预处理天然气(117)膨胀，并且膨胀的天然气(121，127，129)被引入到含至少一个主蒸馏塔(49)的NGL回收单元(19)中，以便一方面生产作为塔顶产物的纯化的天然气(151)，并且另一方面生产所述NGL馏分(15)；和
(d)由来自步骤(c)的纯化天然气(151)形成所述可液化天然气(161)；
其特征在于步骤(a)包括下述子步骤：
(a1)将原料天然气(101)冷却到接近其露点的温度；
(a2)来自步骤(a1)的所述冷却的原料天然气(103)被引入到配有产生回流的塔顶冷凝器(32)的辅助蒸馏塔(31)中，该辅助蒸馏塔(31)在45至65巴的压力下操作，并产生作为顶部产物的所述预处理的天然气(111)，该预处理的天然气(111)基本上不含C6 +烃，这个辅助蒸馏塔(31)此外还产生基本上C6 +重质烃的馏分(105)；
步骤(c)包括下述子步骤：
(c1)将来自步骤(b)的冷却的预处理天然气(117)引入到分离鼓(47)内，以便获得液体流(121)和气体流(125)；
(c2)来自步骤(c1)的气体流(125)在连接到第一压缩机(53)上的涡轮机(51)中膨胀；
(c3)将来自步骤(c2)的流(129)在中间高度N3处引入到主塔(49)内；
(c4)使来自步骤(c1)的液体流(121)膨胀，并将这一膨胀的液体流(121)在高度N3下方的高度N2处引入到主塔(49)内；
并且可液化天然气(161)此外包括直接来自步骤(a)的预处理的天然气(111)的一部分(115)。
2.权利要求1的方法，其特征在于步骤(d)包括下述子步骤：
(d1)在至少第一压缩机(53)中，在液化压力下压缩从所述主塔(49)的项部提取的纯化的天然气(151)；
(d2)在第一换热器(41)中，通过与从主塔(49)顶部提取的所述纯化的天然气(151)进行热交换，来自步骤(d1)的压缩的纯化天然气(155)被冷却，以产生可液化的天然气(161)。
3.权利要求2的方法，其特征在于步骤(b)包括下述子步骤：
(b1)通过在第二换热器(49)中与从第二主塔(49)中提取的纯化天然气(151)进行热交换，来自步骤(a)的预处理的天然气(113)被冷却。
4.权利要求2或3的方法，其特征在于在步骤(d1)中，通过第一压缩机(53)输出的压缩的纯化天然气(153)在通过外部能源(56)供应的第二压缩机(55)中压缩，以达到所述的液化压力。
5.权利要求1-4任何一项的方法，其特征在于主蒸馏塔(49)的压力大于35巴。
6.权利要求1-5任何一项的方法，其特征在于该方法包括启动阶段，其中可液化天然气(161)主要或者完全由直接来自步骤(a)的预处理的天然气(111)组成，所述可液化天然气(161)相对富含C2-C5烃，并且该方法包括随后的生产阶段，其中根据在可液化天然气(161)中所需的C2-C5烃含量来调节在可液化天然气(161)中直接来自步骤(a)的预处理天然气(111)的部分(115)。
7.前述任何一项权利要求的方法，其特征在于通过辅助塔(31)生产的液体(105)被膨胀并被引入到主塔(49)中。
8.前述任何一项权利要求的方法，其特征在于辅助蒸馏塔(31)被设计用来提取存在于原料天然气(101)中的约98mol％的C6 +烃。
9.前述任何一项权利要求的方法，其特征在于在预处理的天然气(111)中C6 +烃的摩尔含量为约等于57ppm。
10.一种用于由含有氮气、甲烷、C2-C5烃和C6 +重质烃的原料天然气(101)同时生产可液化天然气(161)和天然气液体(NGL)馏分(15)的装置，这类装置包括：
(a)用于预处理所述原料天然气(11)以获得预处理的天然气(111)的单元(17)；
(b)用于将预处理的天然气(111)冷却到接近其露点的温度的设备(43)；
(c)用于回收NGL的单元(19)，其包括使冷却的预处理的天然气(117)膨胀的设备(51，123，131)，且包括至少一个主蒸馏塔(49)，所述主蒸馏塔(49)一方面生产纯化的天然气(151)作为塔顶产物，并且另一方面生产所述的NGL馏分(15)；和
(d)用于由来自步骤(c)的纯化的天然气(151)形成可液化天然气的设备(53，55，41)；
其特征在于预处理单元(17)包括：
(a1)用于将原料天然气(101)冷却到接近其露点的温度的设备(25，27，29)；
(a2)用于蒸馏冷却的原料天然气(103)的辅助蒸馏塔(31)，该辅助蒸馏塔配有产生回流的塔顶冷凝器(32)，所述辅助蒸馏塔(31)在45至65巴的压力下操作，并产生所述预处理的天然气(111)作为顶部产物，所述顶部产物基本上不含C6 +烃，这个辅助塔此外产生基本上C6 +重质烃的馏分(105)；
其特征在于，用于回收NGL的单元(19)包括：
(c1)用于分离冷却的预处理天然气(117)的分离鼓(47)，所述鼓产生液体流(121)和气体流(119)；
(c2)用于使所述气体流膨胀的第一膨胀涡轮机(51)，所述涡轮机连接到第一压缩机(53)上；
(c3)用于在中间高度N3处将膨胀的气体流(129)引入到主塔(49)中的设备；
(c4)用于使所述液体流(121)膨胀的设备(123)和用于在N3下方的高度N2处将膨胀的液体流引入到主塔(49)的设备，
并且用于形成可液化天然气(161)的设备包括用于将直接来自预处理单元(17)的预处理天然气(111)的可调节部分(115)选择性地引入到可液化天然气管线(161)中的设备。
11.权利要求10的装置，其特征在于用于形成可液化天然气(161)的设备(53，55，41)包括：
(d1)用于在液化压力下压缩从主塔(49)顶部提取的纯化天然气(151)的设备(53，55)，包括至少第一压缩机(53)；
(d2)第一换热器(41)，所述第一换热器(41)使来自所述压缩设备(53，55)的压缩纯化的天然气(155)与从主塔(49)顶部提取的所述纯化的天然气(151)产生换热的关系，所述压缩纯化的天然气(155)在这个第一换热器(41)中冷却，以产生可液化天然气(161)。
12.权利要求11的装置，其特征在于用于冷却预处理天然气(111)的设备(43)包括第二换热器(43)，所述第二换热器(43)使这种气体(111)与从主塔(49)中提取的所述纯化的天然气(151)产生换热的关系。
13.权利要求11或12的装置，其特征在于用于压缩从主塔(49)顶部提取的纯化天然气(151)的设备(53，55)此外包括通过外部能源驱动的第二压缩机(55)，所述第二压缩机(55)旨在将压缩纯化的天然气(155)的压力提高到液化压力。
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CN101824344A (zh) * 2009-03-04 2010-09-08 鲁姆斯科技公司 氮去除和等压开放式制冷的天然气液回收
CN101824344B (zh) * 2009-03-04 2014-08-06 鲁姆斯科技公司 氮去除和等压开放式制冷的天然气液回收
CN101508925B (zh) * 2009-03-13 2012-10-10 北京永记鑫经贸有限公司 一种天然气液化工艺
CN102762700A (zh) * 2009-12-18 2012-10-31 道达尔公司 具有经调节的总热值的液化天然气生产方法
CN102762700B (zh) * 2009-12-18 2014-11-12 道达尔公司 具有经调节的总热值的液化天然气生产方法
CN103201013A (zh) * 2010-09-03 2013-07-10 缠绕机公司 用于精炼原料气流的精炼系统和方法
CN103201013B (zh) * 2010-09-03 2017-02-22 缠绕机公司 用于精炼原料气流的精炼系统和方法
CN104736504A (zh) * 2012-07-26 2015-06-24 氟石科技公司 用于深度的进料气体烃露点调整的构造和方法

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CA2527381C (fr) 2012-03-13
CA2527381A1 (fr) 2004-12-16
PT1639062E (pt) 2007-08-09
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JP2007526924A (ja) 2007-09-20
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DE602004006266D1 (de) 2007-06-14
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TW200503815A (en) 2005-02-01
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US7237407B2 (en) 2007-07-03
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