CN101852534A - 用于使富含烃类的馏份液化的方法 - Google Patents

用于使富含烃类的馏份液化的方法 Download PDF

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CN101852534A
CN101852534A CN201010154965A CN201010154965A CN101852534A CN 101852534 A CN101852534 A CN 101852534A CN 201010154965 A CN201010154965 A CN 201010154965A CN 201010154965 A CN201010154965 A CN 201010154965A CN 101852534 A CN101852534 A CN 101852534A
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fraction
nitrogen
liquefaction
rich
hydro carbons
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H·施密特
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Linde GmbH
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Linde GmbH
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
    • B01D5/003—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium within column(s)
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    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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Abstract

本发明涉及用于使含有氮气的富含烃类的馏份液化的方法，其中富含烃类的馏份在与至少一个冷却循环的冷却剂或冷却剂混合物方向相反地进行间接热交换的情况下实施冷却及液化，并临时储存经液化的富含烃类的馏份。根据本发明在使富含烃类的馏份液化期间实施氮分离(D、T)，并将在储存(S)经液化的馏份时产生的蒸发气体馏份(8)压缩(V)及返回式液化(E1)，其中蒸发气体馏份与同一冷却循环(20、21)方向相反地进行返回式液化，并且也对该馏份实施氮分离(D、T)。

Description

用于使富含烃类的馏份液化的方法
技术领域
本发明涉及用于使含有氮气的富含烃类的馏份液化的方法，其中富含烃类的馏份在与至少一个冷却循环的冷却剂或冷却剂混合物方向相反地进行间接热交换的情况下实施冷却及液化，并临时储存经液化的富含烃类的馏份。
背景技术
此类用于使含有氮气的富含烃类的馏份液化的方法尤其是用于天然气液化过程，并且早已是在现有技术中已知的。早期通常需要使包含在此类馏份中的所有甲烷液化。其原因是天然气价格高，而且在高效发电站中发电所达到的总效率明显优于通过在燃气轮机中燃烧天然气所能达到的总效率。
通常天然气中的氮含量为1至5体积％。因为储存的经液化的天然气产品(LNG)中允许的氮含量不得超过1体积％的值，仅能很有效地避免非期望的倾翻(Roll-Over)效应，所以此类天然气并未完全液化。
若液化过程的循环压缩机具有电力驱动，而且无法在燃气轮机中燃烧天然气，则在储存LNG时产生的返罐气体(Tankrückgas)或蒸发气体(Boil-Off-Gas)目前就在残气网络(Restgasnetz)中压缩。若不设置残气网络，则试图集成其中可以燃烧残余气体的燃气轮机。
比较大的天然气液化过程例如理解为液化效率大于2mtpa LNG的LNG-基底负载设备，在此过程中借助用于分离出氮气的所谓的脱氮装置(NRU)对蒸发气体进行后期处理。将在此获得的甲烷返回式液化或者作为可燃气体送入燃气轮机。若在较小的液化过程的情况下待液化的粗煤气中的氮含量大于1体积％，则不设置前述的氮分离就无法实现在LNG生产过程中的高的甲烷产率。
发明内容
本发明的目的是提供用于使含有氮气的富含烃类的馏份液化的此类方法，利用该方法可以将甲烷产率提高至接近100％。
为了实现该目的，建议用于使含有氮气的富含烃类的馏份液化的方法，其特征在于，在使富含烃类的馏份液化期间实施氮分离，并将在储存经液化的馏份时产生的蒸发气体馏份压缩及返回式液化，其中蒸发气体馏份与同一冷却循环方向相反地进行返回式液化，并且也对该馏份实施氮分离。
用于使富含烃类的馏份液化的本发明方法的另一个优选的实施方案的特征在于，
-在氮分离期间获得的氮气馏份的残余甲烷含量允许将该氮气馏份排放至大气中或者作为低热量(niederkalorig)可燃气体使用，
-在氮分离期间获得的氮气馏份的残余甲烷含量小于5体积％，优选小于1体积％，
-在至少一个分离机和/或至少一个精馏塔中进行氮分离，其中在设置多个分离机和/或精馏塔的情况下它们优选以级联的方式布置，
和/或在不同的压力下运行，
-将待进行返回式液化的蒸发气体馏份在送至液化过程之前和/或在液化过程中但仍在送至氮分离之前混入待液化的富含烃类的馏份中，
-待进行返回式液化的蒸发气体馏份与待液化的富含烃类的馏份一起压缩，
-将待液化的富含烃类的馏份在氮分离之前分离出重的烃类、C2+烃和/或C3+烃，
-若在至少一个精馏塔中进行氮分离，则将待液化的富含烃类的馏份的支流作为精馏塔的塔底中的汽提气流送入精馏塔或其中至少一个精馏塔，和/或将待液化的富含烃类的馏份的支流在精馏塔或其中一个精馏塔的重沸器中冷却，并作为其他的进料流送入精馏塔或其中至少一个精馏塔，
-若在至少一个精馏塔中进行氮分离，则利用设置在精馏塔中的冷凝器调节由精馏塔排出的氮气馏份中的氮含量。
现在根据本发明已经在富含烃类的馏份的液化过程中进行氮分离。由此降低待液化的富含烃类的馏份中的氮含量，使得(储存的)LNG产品中的氮含量优选低于1体积％。根据本发明对在储存LNG产品时产生的蒸发气体馏份实施返回式液化，从而不会丢失其中所含的甲烷。根据本发明设计氮分离，使得在该过程中获得的氮气馏份中的残余甲烷含量低，以至于该馏份优选在减压及获得制冷之后无需额外的后期处理即可直接排放至大气。
因为在待液化的富含烃类的馏份中所含的所有甲烷原则上均可在LNG产品中获得，所以利用根据本发明的液化方法可以将LNG液化过程的甲烷产率提高至接近100％。
与已知的液化过程不同，不再需要设置额外的用于处理蒸发气体馏份的NRU，其尤其是在较小的液化过程中是不成比例地成本高昂的。
根据本发明设置的氮分离需要更大的能量消耗。但这低于液化过程的总能量需求的10％。此外，除了分离机或精馏塔以外，不需要其他决定成本的机器。
下面依照图1和2中所示的实施例更详细地阐述根据本发明用于使含有氮气的富含烃类的馏份液化的方法及其另外的实施方案。
附图说明
图1所示为在分离机D中实现氮分离的实施方案；
图2所示为本发明方法的实施方案，其中在精馏塔T中进行氮分离。
具体实施方式
将含有氮气的富含烃类的馏份经由管道1送入任选设置的预清洁单元R中。其包括在低的粗煤气压力下预压缩以及通常的去除CO2和汞以及干燥。随后将如此预处理的馏份经由管道2送入热交换器E1，并在其中进行冷却或者已经部分液化。
热交换器E1通常作为板式热交换器或者作为缠绕式热交换器实现。在相应地大容量的情况下，任选设置多个相互平行排列的热交换器。
与至少一个任意实现的在图1和2中仅由用于将冷却剂或冷却剂混合物导入或导出热交换器E1的管道段20和21所图示的冷却循环方向相反地使富含烃类的馏份冷却及液化。冷却循环优选作为膨胀循环(Expander-kreislauf)或混合循环(Gemischkreislauf)而构成。一种或多种用于其中的冷却剂和/或冷却剂混合物可以在热交换器E2中预先冷却和/或在图2所示的实施例的情况下于热交换器E3中加热。
若分离机D上游的压力的大小使得，不减压就不能在分离机D中分离成液相和气相，在阀门a中减压并作为两相流送入分离机D，则经冷却或者已经部分液化的馏份经由管道3从热交换器E1排出。在分离机D的顶部经由管道4排出具有残余甲烷含量的富含氮气的馏份，其可以用作低热量可燃气体。该富含氮气的馏份在阀门b中制冷做功膨胀(
Figure GSA00000078661000041
entspannt)，在此在热交换器E2中利用该制冷，并经由管道5排出至图1中未示出的可燃气体网络。
若待液化的富含烃类的馏份包含较重的烃类，则优选在氮分离之前分离该较重的烃类。该分离可以在SKW分离机、脱乙烷塔、脱丙烷塔等中进行。
若液化过程的周围存在低热量气体的燃烧器，则图1中所示的本发明方法的实施例是特别有意义的。在此情况下，在分离机D的顶部排出的氮气馏份4以获得制冷的方式进行加热(热交换器E2)，及任选在图1中未示出的压缩之后作为低热量可燃气体送至该燃烧器或者该可燃气体网络。
仅代替分离机D，还可设置由多个分离机组成的分离机级联。它的分离机优选在不同的压力下运行，从而更佳地分离含有氮气的富含烃类的馏份，并节省压缩能量。
由分离机D的底部经由管道6排出氮含量低的液体馏份，并在热交换器E1中进一步液化。调节该液体馏份的氮含量，从而在储存的经液化的天然气中存在小于1体积％的氮。这也可能通过额外的在分离机D底部的重沸器而实现，或者通过用作汽提气体的含有氮气的富含烃类的馏份的支流而实现。该汽提气流可以在热交换器E1中预先冷却。经由管道7将如此获得的LNG液体产品在阀门c中减压之后送入储存器S。若从分离机D经由管道6排出的液体馏份已经在液化过程的冷端产生，则还可将其直接送入储存容器S，从而任选设置泵。
现在在储存器S中储存的LNG产品的氮含量小于1体积％。若需要在压缩机V中进行单级或多级压缩，并重新送入液化过程，则将在储存器S中产生的蒸发气体经由管道8从储存器S排出。如图1和2中所示，可以在送至粗煤气压缩和/或热交换器E1之前已经将蒸发气体馏份混入待液化的富含烃类的馏份中，和/或在热交换器E1自身的通道内进行冷却或者部分液化。在各种情况下在送入分离机D或精馏塔T中之前组合引导两种馏份。
图2中所示的本发明方法的实施方案与图1中所示的实施方案的区别在于，代替分离机D设置精馏塔T。本发明方法的该实施方案的优点在于，精馏塔T的塔顶气体4的氮含量可以调节至任意低的值。精馏塔T具有为了调节塔顶气体4的氮含量而提供制冷的冷凝器E3。若塔顶气体4用作低热量可燃气体，则还可将待液化的含有氮气的富含烃类的馏份的支流代替热交换器E3用作外部回流(Fremdrücklauf)。
有利地引导任选经预处理的待液化的馏份的支流经由管道9通过重沸器E4，通过重沸器E4使所储存的LNG产品的氮含量保持在低于1体积％，随后在阀门d中减压，并作为额外的进料流经由管道9′送入精馏塔T。此外还可将待液化的馏份的支流在热交换器E1中部分冷却之前或之后直接用作精馏塔T塔底中的汽提气流。
若经由管道6从精馏塔T排出的液体馏份已经在液化过程的冷端产生，则还可将其直接送入储存容器S，从而任选设置泵。

Claims (9)

1.用于使含有氮气的富含烃类的馏份液化的方法，其中富含烃类的馏份在与至少一个冷却循环的冷却剂或冷却剂混合物方向相反地进行间接热交换的情况下实施冷却及液化，并临时储存经液化的富含烃类的馏份，其特征在于，在使富含烃类的馏份液化期间实施氮分离(D、T)，并将在储存(S)经液化的馏份时产生的蒸发气体馏份(8)压缩(V)及返回式液化(E1)，其中蒸发气体馏份与同一冷却循环(20、21)方向相反地进行返回式液化，并且也对该馏份实施氮分离(D、T)。
2.根据权利要求1的方法，其特征在于，在氮分离(D、T)期间获得的氮气馏份的残余甲烷含量允许将该氮气馏份排放至大气中或者作为低热量可燃气体使用。
3.根据权利要求1或2的方法，其特征在于，在氮分离(D、T)期间获得的氮气馏份的残余甲烷含量小于5体积％，优选小于1体积％。
4.根据权利要求1至3之一的方法，其特征在于，在至少一个分离机(D)和/或至少一个精馏塔(T)中进行氮分离(D、T)，其中在设置多个分离机和/或精馏塔的情况下它们优选以级联的方式布置，和/或在不同的压力下运行。
5.根据权利要求1至4之一的方法，其特征在于，将待进行返回式液化的蒸发气体馏份(8)在送至液化过程之前和/或在液化过程中但仍在送至氮分离(D、T)之前混入待液化的富含烃类的馏份(1)中。
6.根据权利要求1至5之一的方法，其特征在于，待进行返回式液化的蒸发气体馏份(8)与待液化的富含烃类的馏份(1)一起压缩。
7.根据权利要求1至6之一的方法，其特征在于，将待液化的富含烃类的馏份(1)在氮分离(D、T)之前分离出重的烃类、C2+烃和/或C3+烃。
8.根据权利要求1至7之一的方法，其中在至少一个精馏塔中进行氮分离，其特征在于，将待液化的富含烃类的馏份的支流(9、9′)作为精馏塔(T)的塔底中的汽提气流送入精馏塔(T)或其中至少一个精馏塔(T)，和/或将待液化的富含烃类的馏份的支流(9、9′)在精馏塔(T)或其中一个精馏塔(T)的重沸器(E4)中冷却，并作为其他的进料流送入精馏塔(T)或其中至少一个精馏塔(T)。
9.根据权利要求1至8之一的方法，其中在至少一个精馏塔中进行氮分离，其特征在于，利用设置在精馏塔(T)中的冷凝器(E3)调节由精馏塔(T)排出的氮气馏份(4)中的氮含量。
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Application publication date: 20101006