CN85109210A - 从分流中分离出c3+—碳氢化合物的方法 - Google Patents

从分流中分离出c3+—碳氢化合物的方法 Download PDF

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CN85109210A
CN85109210A CN85109210.1A CN85109210A CN85109210A CN 85109210 A CN85109210 A CN 85109210A CN 85109210 A CN85109210 A CN 85109210A CN 85109210 A CN85109210 A CN 85109210A
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萨珀尔·雷纳
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Abstract

建议了一种从天然气或类似的气流中分离出C3+—碳氢化合物的方法。处在压力下的气体，使其通过冷却进行部分冷凝。使气体的馏分减压作功，通过精馏分离液相馏分。由作功减压的气体馏分通过洗涤分离其他的C3+—碳氢化合物，并且同样地送去精馏。洗过的馏分其压力高于精馏压力，可以作为C2+—流出产物提供出来。

Description

本发明是关于从一种主要含有轻的碳氢化合物的气流中分离C3+-碳氢化合物的方法，在此方法中使处在高压下的气流冷却，部分冷凝并分离成一种液体的馏分和一种气体的馏分，在此方法中使该气体馏分减压作功，该液体馏分通过精馏分离成一种主要含有C3+-碳氢化合物的产品流出物和一种主要含有较轻沸点组分的剩余气体馏分。
该种方法，举例来说，用来从天然气或炼厂气获得液化石油气馏分（C3/C4-碳氢化合物），或者用于丙烷和较高碳氢化合物的分离，有时也用于从炼厂气或裂化气提取不饱和的碳氢化合物。在较早的，未公开的德国专利申请P3408760，5中，已经描述了一种这类方法。这种较早申请的主要特征在于，部分冷凝后剩余气体馏分减压作功产生的致冷量不用在精馏时制取回流液体，而是用于原料气的冷却和部分冷凝。因此无需将气流的轻的部分送去精馏。进料的轻的部分（特别是C1-和C2-碳氢化合物）不进入分离塔，可以使精馏在一较高的温度下进行。在精馏时塔顶冷却可能使用简单的经济实惠的外冷却循环，尽管这种可能性意味着是一种方法程序很大的改善，但是仍然还希望能有进一步的改良。特别是希望分离出的C3+-碳氢化合物的产率进一步提高，在这当中无需将全部气流送去精馏或者在较低的温度下进行部分冷凝。若C2-馏分应当在高压下提供时，若需要很大的压缩功将轻馏分再压缩时，这对已知的方法也是特别不利的。
因此发明的基础任务是，开始提到的这类方法是这样实现的，使使其能够以较少的化费分离C3+-碳氢化合物，并且至少部分地避免所提到的缺点。
这个任务是通过如下的方式得到解决的：通过洗涤从作功减压的气体馏份中分离出其余的C3+-碳氢化合物，并且同样地送去精馏，与此同时由洗涤出来的气体馏分重新被加热，并且作为主要含有C2--碳氢化合物的产品流出物提供出来。
在老的方法中是减压作功的气体馏分直接与要冷却的气流逆流被加热，然后作为产物气体放出来，则本发明是通过洗涤将其中还含有的重组分分离出来，并送去精馏以制取C3+，由此直接得到一较高的C3+-碳氢化合物产率。
在一优选的发明实施中，洗涤是在一个比精馏更高的压力下进行的，也就是说，进行作功减压没有达到精馏压力。若是应当加热以后在高压下提供C2--馏分，这种作法证明是特别有利的，因为由此所需花费的重新压缩能量是很少的，或者在最理想的情况下可以完全去掉。
尽管有一些其他的洗涤剂，特别是碳氢化合物的混合物在这里也适用，洗涤主要是用本方法附带产生的一种碳氢化合物的混合物进行的。在一个特别优选的发明实施中，洗涤是使用一种由精馏剩余气部份冷凝获得的洗涤剂进行的。在这当中剩余气的部分冷凝可以通过与任意一种温度比精馏塔顶温度更低的本方法中的流出物或冷却剂换热而得以实现。
在这当中主要的只是须注意，生成的冷凝物数量，要为得到所希望的C3+-产率准备足够的洗涤剂。因为在部分冷凝时仍含在剩余气中的C3+-碳氢化合物首先冷凝，并且在通过洗涤以后又返回精馏，因此没有与剩余气一起完全丢失，所以剩余气用作洗涤剂也是特别适宜的。
在本发明方法的一个优选的实施中，剩余气体的部分冷凝，是通过与汽化的洗涤塔底液体产物换热进行的。在一种特别优选的这种方法演变的发展类型中，洗涤和精馏的压力是这样互相协调的，使剩余气不预先压缩与汽化的洗涤塔顶产物逆流进行部分冷凝。这种方法步骤主要是后来在精馏压力下进行的。此外实施这种方法时，将部分冷凝的剩余气体进行一次相分离，并且只将液相送到洗涤，是适宜的，为此通过一种简单的运转耗能不大的液泵在洗涤压力下输送该液体。剩余气没有冷凝的部分可以在与要冷却的流程中的流体逆流加热以后作为单独的流出产物，例如作为燃料气，在精馏压力下（去掉大约在管道和热交换器中流动时不可避免产生的压力降）提供出来。
由洗涤出来的C2--馏分具有很大的潜冷量，该潜冷量可首先在比较适当的发明的发展方法中这样利用，使它用于精馏塔顶冷却，并且以后再与要冷却的气流换热。
不仅部分冷凝生成的液相而且洗涤塔底产物都送去精馏。在这当中，在精馏以前进行一次这些馏分的部分汽化是有利的，例如，这种汽化可以与由精馏来的冷凝剩余气和/或与要冷却的气流通过换热实现。这二种液体馏分可以分别送入精馏，在这当中进料是取决于液体馏分组成和精馏内部的平衡曲线。将这种馏分膨胀以后混合使其达到一总的压力高度，并且在进入精馏以前至少部分地共同加热，当然常常是比较简单的，尤其是在液体馏分组成互相只有很少差别时。
本发明的方法特别适于处理相对来说轻的气流，也就是说一种含有许多C1-和C2-碳氢化合物的气流，若是该种C1/C2-气体产物应在高压下提供时。尤其是天然气可以理解为轻的气体，其甲烷和乙烷组分超过90%。加工这种气体时，不仅洗涤而且精馏都是在尽可能高的压力下进行的。因为这里分离出大量的例如要放到天然气管道的出售气体，因此在洗涤段优选用了高压。由于洗涤段的高压大大的减少了所需的再压缩功。因为要液化大部分由塔顶得到的剩余气体作为洗涤剂送往洗涤段，同时因为这种液化主要应当是对剩余气体不进行预先压缩，所以在精馏段选用了高压力。洗涤的通用压力在35到45巴之间，例如在43巴，对于精馏压力为25到32巴之间，例如在30巴。在加工一种轻质天然气时，若力求取得一种液化气作为要分离的C3+-馏分时，该液化气具有液化石油气的性能，并且由大约30%的丙烷和70%的丁烷组成，该方法就特别适用。在这样一种实施形势中努力追求达到一种很高的C4+-碳氢化合物分离度，与此同时C3-产率，相对来讲，是低的，例如丙烷是含在气流中的20%到60%。
发明的其他细节在下面以一个在图中描述的流程实施例加以说明。
在图中所描述的实施例中，在压力为69巴和温度为315K时，由管道1输入一种天然气，该气含有92.6%的甲烷（百分数为mol-%），4.3%的乙烷，1.3%的丙烷，0.55%的丁烷和0.25%的C5+-碳氢化合物以及1.0%的惰性物质（氮和二氧化碳），并且在一热交换器中，与要加热的流程中的流体逆向冷却到234K。这种在冷却时部分冷凝的天然气，由管道3抽出，并在分离器中进行相分离。冷凝物经管道5放出，它含有1.2%的Co2，54.0%的甲烷，11.5%的乙烷，9.6%的丙烷，9.8%的丁烷和1.39%的C5+-碳氢化合物。在阀门6处减压到压力为大约30巴，并且在换热器7中部分加热以后，与一尚须描叙的流程中的流体混合。由分离器4经过管道8抽出一气体状的馏分，该馏分在膨胀透平9中膨胀到压力为43巴，在这当中该气体冷却到211K。在膨胀时在气体中仍含有的C3+-碳氢化合物的较大部分在二相的出口流出物的液相中进行冷凝，这种作法有助于使方法得到高产率。将此二相混合物导入洗涤塔11的下部区域，在塔中用一种尚须叙述的液体对这种混合物进行冲洗。通过洗涤分离出其余的C3+-组分以后，在洗涤塔顶经过管道12引出一种轻的气体，该气体在精馏塔14的换热器13中由210K加热到214K以后，经管道15引出，在换热器2中与要冷却的天然气逆流被加热到302K。接着这种气体经过管道16到达一压缩机17，该压缩机通过一根轴18由膨胀透平9所驱动，接着经过管道19进到一压缩机20，在此压缩机中气体被压缩到输出压力为72巴。在换热器21中在压缩热冷却以后，在315K的温度放出这种气体。
由洗涤塔11的塔底经过管道22在温度为211K引出一液体，它含有1.6%的二氧化碳，57.5%的甲烷，16.9%的乙烷，14.5%的丙烷，8.8%的丁烷和0.7%的C5+-碳氢化合物。这种液体在阀门23减压到大约30巴的压力，接着在换热器7中加热，然后与同样在换热器7中加热的由分离器4来的冷凝物混合，并经过管道24送到换热器2，在此与冷却的天然气逆流进行进一步的加热。在温度为302K时这种液流，它后来分为二相，经过管道25进入精馏塔，在塔内C3+-碳氢化合物从较轻的组分中分离出来。由塔底经过管道26放出C3+-产物馏份，该馏分含有1.3%的乙烷，28%的丙烷，49.1%的丁烷和21.6%的C5+-碳氢化合物。将精馏塔底产物的一部分经过管道27分出，在换热器28中加热，并且作为塔底加热重新送回塔14的下部区域。在精馏塔的塔顶过滤器的上面，该过滤器应防止液体颗粒的带出，在温度为261K时附带产出一种经过管道30放出的塔顶产物，它含有1.9%的二氧化碳和氮，68.1%的甲烷，19.5%的乙烷和10.5%的丙烷，并且只还有100ppm C4+-碳氢化合物没有搞净。这种气体不用预先压缩在换热器7中，与由洗涤塔11来的减压到精馏压力的塔底产物逆流，并且与由分离器4来的同样减压到精馏压力的冷凝物逆流部分地被冷凝，接着送到分离器31中，在分离器中进行相分离。冷凝部分经过管道32放出，在它进入洗涤塔的上部区域之前，通过泵33输送，压力提高到洗涤塔的43巴。在分离器31产生的没有冷凝的气体，经过管道34放出，并且在换热器2中与要冷却的天然气逆流加热以后，经过管道35作为剩余气体，该剩余气体例如可以用作燃料气，在压力为30巴和温度为302K时被提供出来。它含有1.3%的氮和二氧化碳，92.8%的甲烷，5.4%的乙烷和0.5%的丙烷。
经过管道26放出的C3+-产物，它是在温度为396K时产生的，含有经管道1引来的气体中所含C4+-碳氢化合物的99.4%，与此同时丙烷的产率大约为25%。

Claims (9)

1、从一种主要含有轻的碳氢化合物的气流中分离C3+-碳氢化合物的方法，在此方法中使处在高压下的气流冷却，部分冷凝并分离成一种液体的馏分和一种气体的馏分，在此方法中使该气体馏分减压作功，该液体馏分通过精馏分离成一种主要含有C3+-碳氢化合物的产品流出物和一种主要含有较轻沸点组分的剩余气体馏分，其特征在于，由作功减压的气体馏分通过洗涤分离其余的C3+-碳氢化合物，并且同样的送去精馏，与此同时，重新加热由洗涤来的气体馏分，并作为主要含C2--碳氢化合物的产品流出物提供出来。
2、根据权利要求1的方法，其特征在于，洗涤是在比精馏更高的压力下进行的。
3、根据权利要求1或2的方法，其特征在于，洗涤是用一种通过精馏剩余气体的部分冷凝得到的洗涤剂进行的。
4、根据权利要求3的方法，其特征在于，剩余气体的部分冷凝是通过与汽化的洗涤塔底产物的热交换实现的。
5、根据权利要求1至4之一的方法，其特征在于，剩余气体的部分冷凝是在精馏的压力下实现的。
6、根据权利要求3至5之一的方法，其特征在于，将部分冷凝的剩余气体进行相分离，并且只用液相作为洗涤剂。
7、根据权利要求6的方法，其特征在于，将液体馏分用泵增压到洗涤的压力。
8、根据权利要求1至7之一的方法，其特征在于，由洗涤来的气体馏分用来冷却精馏塔顶。
9、根据权利要求1至8之一的方法，其特征在于，在剩余气体部分冷凝以分离的液体馏分与洗涤塔底产物混合，并且同它一起在输入精馏之前进行加热。
CN85109210.1A 1984-12-17 1985-12-16 从分流中分离出c3+-碳氢化合物的方法 Expired CN1003600B (zh)

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