CN85109187A - 提取c2+或c3+烃的方法 - Google Patents

提取c2+或c3+烃的方法 Download PDF

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CN85109187A
CN85109187A CN85109187.3A CN85109187A CN85109187A CN 85109187 A CN85109187 A CN 85109187A CN 85109187 A CN85109187 A CN 85109187A CN 85109187 A CN85109187 A CN 85109187A
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鲍尔·海因茨
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Abstract

本发明提出了一种适用于从主要含易挥发的烃，也可能含氢或氮的气体混合物中提取C2+或C3+烃的方法。先将气体混合物冷却而进行分相，然后将凝结的组分进行精馏。气体中的不凝结部分用精馏塔的塔顶产物分凝成的液体处理以洗涤出其中含有的C2+或C3+烃。洗涤所产生的液体作为精馏过程的外来回流而洗涤后的残余气体加热后排出。

Description

本发明涉及从气流中提取C2+及C3+烃的方法。该气流含易挥发的烃，有时还可能含沸点低于甲烷的物质。本方法是将高压下的气体冷却使之部分冷凝，分成液相及气相两部分并从通过精馏将液相分解成含C2+或C3+烃的产物和主要含其他易挥发组分的剩余气流。
这类方法主要用于从天然气或其他气体例如炼油厂的废气中分离出乙烷或丙烷。此外也可用来提取类似的不饱和烃，例如乙烯或丙烯。炼油厂的废气中就可能含这些组分。近年来由于LPG（C3/C4烃混合物气体）的市场价格提高，而真空炼油炼油残渣及重油则不易售出，所以进一步加工炼油厂的废气使具有了一定的经济价值。因此，不易出售的重油产品就用来作燃料，而从废气中提取畅销的C2+及C3+碳氢化合物。这种废气在从原油的轻油成份中提取汽油时大量产生。
在较早的未公开的德国专利申请P3408760.5中曾描述过一种关于提取C3+烃的方法。这个老申请的一个主要特征是，要求提取的C3+碳氢化合物在分凝时已几乎全部凝结，只将冷凝液进行精馏。而未凝结气体中含C3+碳氢化合物很少不值得再进行加工，因而不再将它经过精馏而直接加热排空。这样处理的优点是可以选择较佳的精馏条件，特别是塔顶温度可选得较高一些。
本发明的任务是将上述方法加以改进，特别是应提高C2+或C3+烃的得率。
完成这一任务的方法是将分凝后分离出的气相馏分导入回收洗涤塔，用精馏时分凝后产生的残余气体洗去气相馏分所含的C2+或C3+烃。将回收洗涤塔塔底收集的液体馏分导回精馏塔。
通过本发明的方法可在回收洗涤塔中比较充分地将C2+或C3+烃分离出来。特别值得惊奇的是，用比较易挥发的馏出物在接触过程中能使还遗留在气体中的难挥发组分凝结。通常都是用比较难挥发的物质作为洗涤剂来洗涤出气体中的某一烃类的。
本发明的方法之所以能达到高的得率是由于许多因素的共同作用。其中有精馏塔产生的残余气体经过分凝后作为制冷剂。它在进入回收洗涤塔时，由比较高的分压降为低分压。所形成的冷凝由于减压而部分蒸发产生制冷作用。所达到的温度较原料气流在分凝时的最低温度还要低得多，从而促使气体中遗留的难挥发组分冷凝下来。另外，回收洗涤塔中能达到的分离度较单纯由于冷却所能达到的要高得多，必然还有别的因素在起作用。特别是溶解度在这里能产生有利的影响。
本发明的另一个有利措施是将回收洗涤塔塔底收集的液体作为精馏塔的回流液。这样还可节省精馏塔为了产生回流液而消耗的外加冷却能量。
本发明还有一个有利措施。一般情况下，回收洗涤塔的塔顶产物是作为废气被加热到室温后放空。本发明则先将它减压，将它用于回收洗涤塔的塔顶冷却。这种附加冷却增大了回收洗涤塔的塔顶冷却程度而进一步提高了过程的得率。减压可简单地让气流通过节流减压阀。如果气流量比较大，或含易挥发组分比较多，例如含氢在20%以上，用膨胀汽轮机减压也是可行的。
本发明的另一种有利方案是分凝后分离出的气相馏分在导入回收洗涤塔之前通过有一次间接换热冷却到更低的温度。这样在气体中遗留的C2+或C3+烃的大部分将凝结而被分离出，并在需要时导入精馏塔，只将未凝结的气体导入回收洗涤塔。将回收洗涤塔塔底收集的液体作为精馏塔的回流液时，上述操作方式特别有利。因为气体中含有的难挥发组分已提前析出，大部分不进入所形成的回流液中。这部分液体可在精馏的适当部位进料，而不需从塔顶加入。
上述方案的一种较好的措施是将间接换热时从气体中析出的冷凝物与从原料气流分离出的液相部分一同送入精馏塔。两种冷凝液分别处理和分别进料虽然也可行，但获得的效益甚微，通常还不足以弥补设备上多支出的费用。将两部分冷凝液公同处理可用一个十分简单的装置，即在用来分离第一次分凝时产生的气液相的分离器中进行再一次冷却及分凝，在分离器上部安装一个换热器可使两种冷凝液进行混合而不需其他结构措施。
精馏塔产生的残余气体的冷却和分凝一般要求冷却到使50%到99%的液相凝结下来的温度，特别有利的是70%到95%，例如90%左右。用一般方式取C3+烃时，残余气体中含少量氢（只要气流中含有氢），甲烷，C2+烃物为其主要成分，少量C3+烃。个别情况下残余气体的组成差别很大，与被处理的原料气体的特殊组成以及操作中所选择的具体操作条件有关。提取C2+烃时，组成分布将偏移到以甲烷为主要成份，只含少量C2+，残余气体中几乎不含C3+烃。残余气体至少要冷却到原料气流分凝时的温度范围才能达到要求的分凝效果。冷却残余气体时可以占用冷却原料气流所用的换热器的一部分，也可单独用一个换热器。
回收洗涤塔的塔顶温度应调节到明显低于气体分凝后的温度，例如低10～20℃。如果直接将回收洗涤塔塔顶产生将作为残余气体加热后排空的气体引入用来冷却原料气流的换热器中，就会造成换热器的冷却端温差相当大，从而热损失也很大。为了避免这种损失，本发明在另一种方案中建议最少将一部分回收洗涤塔的塔顶产物先与换热器中已部分冷却及分凝的精馏塔产生的残余气体进行热交换。这样不仅避免了冷却原料气流的换热器的冷端温差大的现象，还增大了精馏塔残余气体的冷却及分凝作用。
本发明的另一有利方案是原料气流分凝出的液体在进入精馏塔前先用需冷却的气流略为加热，然后将形成的气液混合物在精馏塔的适当部位导入。
沸点低于甲烷的组分在所处理的原料气流中含量较大时，本发明有另一种方案来增加这些组分的含量，即从回收洗涤塔的塔顶产物中通过分凝分离出C1及C2烃。例如从富含氮的天然气中提取C2+或C3+烃和氮，特别是从富含氢的炼油厂废气中提取上述难挥发的烃及氢可采用这种操作方式。当原料气流中含低沸点组分相当多时，这种操作方式的优点显示得特别突出。例如氢含量在50%到90%范围时，所含的氢在减压时所产生的制冷能力已足够用来进行附加的分离操作而不必使用外加的能量。
许多应用实例中还要求将C2+或C3+烃产物分离，特别是C3/C4混合烃和C5+烃的分离，为此目的，本发明的操作过程中有一个先进措施就是在产生液相及气相之前先将C5+烃从气流中析出。条件是这些组分的含量足够大，值得进行这种分离。
比较适当的分离C5+烃的方法是在温度高于形成前述的气相及液相馏份的温度时使之分离出。除去难挥发的组分后，进入精馏塔的混合物几乎不含C5+烃，所以此后对液体馏份进行精馏可得分离出C3+即为市场上出售的LPG馏份的产品料流。
为了提高C3及C4烃的得率，本发明还可进一步改善。即将分离出的难挥发烃也导入精馏塔中。但加料点按照精馏塔中的平衡过程安排在塔上分凝时形成的液相分凝物进料点的下方，并在两个加料点之间将主要含C3及C4烃的馏份侧线引出。由于C5+馏份参加精馏过程，C5+馏分分凝时溶解在溶液中的C3/C4烃还可以回收。精馏塔中在两个加料点之间形成一个C3/C4浓度最大的区域，最好是在这个位置上将C3/C4产品取出。
实现本发明方法的设备中作为主要部件最少有一台换热器用来冷却原料气流并使之分凝一台分离器分离从气凝中分凝出的液体部分，一个精馏塔将分凝的液体部分进行精馏，一个回收洗涤塔，它的下部与分离器的蒸汽室相通，而上部则与精馏塔的塔顶相连接，精馏塔塔顶与回收洗涤塔上部之间还装上一个换热器。
这种设备的一种特别有利的结构是将分离器与回收洗涤塔放在同一容器中。比较有利的方式是回收洗涤塔装在分离器的上面而用一个烟囱形底板隔开，使从分离器排出的气体经过烟囱隔板进入回收洗涤塔的下方。更进一步的结构是在分离器的上部装换热管，用操作中产生的冷气流或其他介质将气相馏份中的难挥发组分在进入回收洗涤塔之前再一次分凝出。
发明中的其他细节可借助于示意图及下面所列举的实施进行说明。
图1表示本发明方法的第一个实施形式。
图2表示本发明方法的另一实施方案，其中附加了一个C5+烃分离级。
图3表示本发明方法的又一实施方式，其中分离器与回收洗涤塔组合成一个部件。
图4表示上述方案的另一种实施形式。
图1示出的实施例中，在高压及接近室温下要求分离的气流经导管1进入换热器2冷却到绝大部分待提取的烃，即C2+或C3+烃冷凝分凝后的气流在分离器3中发生相分离。凝结的液体经导管4到换热器2部分蒸发后进入精馏塔5，在精馏塔5中分离出的C2+或C3+馏份作为塔底产品从导管6抽出，含易挥发组分的残余气体则经导管7排出。精馏利用从导管8导入的外来回流的及塔底加热器9进行。加热可采用如低压蒸汽或热水。
经导管7导出的精馏塔塔顶产物主要为沸点较由导管6导出的馏份低的组份。它进入换热器2并重新冷却后可使其中仍含有的较难挥发的组分部分凝结。形成的冷凝液量一般大于精馏塔所需的回流液量。部分冷凝后的残余气体将被导入回收洗涤塔10的上部，在此与分离器3经导管11引入的气流进行逆流接触，塔10的塔底收集的液体从导管12流出，用泵13经导管8送到精馏塔5作为外来回流。回收洗涤塔的塔顶产生的气体经导管14抽出，其中几乎完全不含需要提取的C2+或C3+烃。这一气流经过减压阀15减至要求的气压，所产生的制冷能量在冷井16中传递到回收洗涤塔10中的气体，然后经过换热器2被加热到室温而从导管17抽出。
在按图1的一个具体的实施例中，流经导管1的原料气流温度为313K，压力为20巴（bar）。其中含15%氢（百分数为摩尔百分比，下同），3%氮，37%甲烷，26%乙烷，14%丙烷，4%丁烷，1%戊烷。在换热器2中被冷却到237K后在分离器中分离出冷凝液，其含0.4%氢，0.2%氮，9.4%甲烷，38.5%乙烷，36.3%丙烷，12.1%丁烷，3.1%戊烷留下的气体部分在回收洗涤塔10中与从精馏塔来同样被冷却到237K的残余气体接触来自导管7的残余气体中含0.5%氢，0.3%氮，15.0%甲烷，80.8%乙烷，3.4%丙烷。回流洗涤塔的塔顶产物在221K的温度下经导管14抽出，流经减压阀15后被减压到残余气体的压力，在冷井16中被加热到218K接着在换热器2中被加热到310K再经导管17在压力5巴的条件下作为排放气体排出。气体中含18.6%氢，3.7%氮，45.8%甲烷，31.7%乙烷，仅含0.2%丙烷。
经导管12导出的回收洗涤塔10的塔底液体产物中含0.3%氢，0.2%氮，10.5%甲烷，7.4%乙烷，14.2%丙烷，0.8%丁烷及戊烷。液体被导入在18巴的压力下操作的精馏塔5的顶部。精馏塔的塔底产物经导管6作为C3+产品排出，其中含2.02.0%乙烷，71.9%丙烷，20.9%丁烷，5.2%戊烷。本法的C3+得率为98.9%。
图2所示的实施例是本发明方法的一种方案。其中第一个步骤是从混合气体中分离C5+组分。入口流体1进入换热器2中首先只冷却到能使绝大部分C5+组分凝结的程度。部分冷却的混合物在某一中间温度离开换热器2进入分离器20，进行分相后，冷凝液从导管21排出，流经换热器2稍被加热后经导管22导入精馏塔。气体部分则流经导管23继续冷却后进入分离器24，它相当于前一方案中的分离器3。
分离器20及分离器24中分离出的冷凝液都在精馏塔25中进行分馏，与前一方案中的精馏塔的差别是这里的塔板数要多一些。两个进料管4及22之间装有出料管26，它的位置在C3/C4的浓度最高处。精馏塔25的塔底产物中主要含C5+烃，它经导管27作为产品抽出。与前一方案相同，在塔25的顶部经导管7排出易挥发组分，它主要含C1及C2烃。
这一方案将先在分离器20中分离出难挥发的组分也导入精馏塔中，用这种方法只增加了比较少的费用而达到很高的C3及C4烃得率。
图3所示的实施例中，原料气流经导管28引入，其温度为305K，压力为28.9巴。气流中含67.5%氢，11.8%甲烷，8.8%C2，7.8%C3，3.3%C4，及0.8%C5+烃。在换热29中被冷却到230K，方法是与操作过程中需要被加热的流体以及图中用导管30示意的制冷循环液进行间接换热。部分冷凝后的混合物经导管31导入分离器中，该分离器安装在容器32中的下部，容器的上部形成一个回收洗涤塔。液相从分离器经导管33抽出，其中含有1.4%氢，3.5%甲烷，23.0%C245.1%C3，21.5%C4及5.5%C5+烃，釜液用泵34在30巴的压力下送回换热器29，稍加热后作为精馏塔35的进料，在精馏塔35中被分馏成塔底的C3+产物及C2-馏出物。塔底的C3+烃经导管36排出，其中一部份流经导管37，在蒸馏釜38中被加热导回精馏塔35的下部。导管36中的产物温度为362K，压力29巴，组成为2.0%C2-，63.6%C3，27.5%C4及6.9%C5烃。精馏塔35的塔顶产物中含2.8%氢，8.7%甲烷，84.4%C2及4.1%C3烃。这一馏份经导管39抽出，冷却后导入回收洗涤塔。冷却先在换热器29中进行，约冷却到230K的温度，然后在换热器40中冷却到202K。这时馏出物中已绝大部分冷凝，经导管41将它导入位于容器32上部的回收洗涤塔的塔顶内。在回收洗涤塔和它下方的分离器之间的烟囱形隔板42上（隔板在回收洗涤塔的下部）收集的液体中，一方面含有精馏塔的塔顶产物，只要它在换热器29及40中冷凝后在回收洗涤塔中没有再蒸发，另一方面还含有从分离器来的气流中洗涤下来的难挥发组分。从分离器分离出的气体部分经过烟囱底板42直接进入回收洗涤器的下部。烟囱形隔板42上收集的液体经导管43抽出，用泵44送至精馏塔35的顶部作为回流。回流液的温度为200K，组成为1.5%氢，6.0%甲烷，78.6%C2，13.6%C30.3%C4烃。
从回收洗涤塔中排出的残余气体经导管45后分成两股气流。一股分流经导管46进入换热器40用来冷却从精馏塔来的塔顶馏出物，约从230K冷却到202K。另一股分流经导管47进入分离器的上部将它的最强的冷却效能传递给分离器中的气相馏份。在分离器中稍被加热后，导管46及47中的分支气流在48处又会合在一起。经过汽轮机作功减压到设备的残余气体排出端要求的排放压力。因减压而冷却的气体经导管50再一次通过分离器的气体空间后经导管51进入换热器29与过程中几种要求被冷却的流体换热，它本身将被加热到302K，最后在压力为17巴的条件下从导管52中排放。该气体含76.8%氢，13.3%甲烷，9.8%C2及0.1%C3烃。
在这种方法中，原料气流中的C3烃有99.5%收集到精馏塔35的塔底而经导管36作为产品排出。
图4所示的方案是图3和前述方法所示方案的一个变体。因此，这里仅介绍其中的程序差别。按照图4，精馏塔35的塔顶产物经导管39导入换热器53中，先与分离器底部产物换热，该产物在被加热后进入精馏塔35中;然后与回收洗涤塔的塔顶产物进行热交换，后者从导管46分支出。回收洗涤塔塔顶产物的支流46从换热器53引出后经导管54直接进入换热器29被加热到室温。这样，从导管55排放的气体仍保持在回收洗涤塔中的压力，只是在导管及换热器中由于不可避免的压力损失而稍有降低。回收洗涤塔的塔顶产物的另一个经导管47分开的支流先在分离器的上部被冷却，然后经导管56进入第一个膨胀汽轮机57减压到中等压力并将获得的制冷能力传递给分离器中的气体部分。气体从汽轮机排出后经导管58重新进入分离器上部的换热器中。从换热器出来的气体再经导管59进入第二个膨胀汽轮机60作功减压，经导管61再一次进入分离器的上部将其制冷能力传递给分离器中的气相部分。最后，残余气体经导管62进入换热器29并作为低压排放气体由导管63排出。
提炼C2+或C3+烃时的精馏条件，如压力及温度一般应根据不同的边界条件进行选择，特别要考虑到所精馏的混合物的组成。此外所处理的气体混合物也可能在不同的条件下，特别是不同程度的高压下供应。个别情况下，分离程序的最佳条件要求精馏塔中的压力高于或低于分凝气流的压力。按照图1到图4所示的实施例是假定这里不存在明显的压差。如果个别情况下存在这种压差，也可在所述的程序中将条件稍加改变即能适应。例如精馏塔中压力较高时，导管4上安排的泵可选择压缩比较高的泵代替一般的输送泵13，并使分凝后的残余气体减压进入回收洗涤塔10中（图1及图2）。

Claims (17)

1、从气体中分离C2+或C3+烃的方法，该气流含易挥发的烃，还可能含沸点低于甲烷的物质，先将高压下的气体冷却，使之部分冷凝分成气相及液相，再将液相精馏分离成主要含C2+或C3+烃的产品和主要含其他易挥发物质的残余气体，本方法的特征是将部分冷凝后分离出的气相部分导入回收洗涤塔，用以从精馏塔得到的部分冷凝后的残余气体洗涤出C2+或C3+烃，并使回收洗涤塔的塔底形成的液相馏分流入精馏塔。
2、根据权利要求1的方法，其特征是回收洗涤塔塔底的液相馏分作为回流液导入精馏塔中。
3、根据权利要求1或2的方法，其特征是，回收洗涤塔的塔顶产物减压后用来冷却本塔的塔顶。
4、根据权利要求1至3中一项的方法，其特征是，原料气流及残余气体的部分冷凝，通过冷却到同一个温度范围来实现。
5、根据权利要求1至4中一项的方法，其特征是，部分冷凝后分离出的气相先与过程中产生的较冷流体进行间接换热而冷却并分离出凝结的成分导入精馏塔，未凝结的气体则导入回收洗涤塔。
6、根据权利要求5的方法，其特征是，气相间接换热时产生的冷凝液与分凝得到的液体合并一同导入精馏塔。
7、根据权利要求6的方法，其特征是，间接换热在专为气液分离而设置的分离器上部进行。
8、根据权利要求1至7中一项的方法，其特征是，精馏塔产生的残余气体在导入回收洗涤塔之前使之50～99%，较好的是70～95%液化。
9、根据权利要求8的方法，其特征是，最后换热阶段的残余气体与从回收洗涤塔产生的气体间接换热以使进一步液化。
10、根据权利要求1至9中一项的方法，其特征是，进入精馏塔前的液相馏分至少要被需冷却的气流部分加热。
11、根据权利要求1至10中一项的方法，其特征是，所处理的气流中富含沸点低于甲烷的组分时，回收洗涤塔的塔顶产物在减压前通过分凝将C1及C2烃除去。
12、根据权利要求1至11的方法，其特征是，如果原料气流中含C5+烃，在气、液相形成之前，将其大部分分离出去。
13、根据权利要求12的方法，其特征是，将分离出的C5+烃同样导入精馏塔，其进料点在分凝液体的进料点以下，而在两个进料点之间抽出主要含C3及C4烃的流体。
14、实施根据权利要求1至13中一项的方法，所用的设备，其中最少有一台换热器用来冷却气流并使其分凝，一台分离器将气流中分凝的液体分离出来，一个精馏塔分馏被分离出来的液体，本发明的特征是：有一台回收洗涤塔，塔的下部与分离器的气体空间连通，上部则与精馏塔的塔顶相联接，精馏塔塔顶与回收洗涤塔上部之间装有一台换热器。
15、根据权利要求14的设备，其特征是，分离器与回收洗涤塔安装在同一容器中。
16、根据权利要求15的设备，其特征是，回收洗涤塔安装在分离器的上方，并用一块烟囱形的隔板将它们隔开。
17、根据权利要求14至16中一项的设备，其特征是，分离器的上部装有换热管。
CN85109187.3A 1984-12-17 1985-12-17 提取c2+或c3+烃的方法 Expired CN1003650B (zh)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101952003A (zh) * 2007-03-06 2011-01-19 林德股份公司 分离方法
CN105783421A (zh) * 2016-04-07 2016-07-20 成都赛普瑞兴科技有限公司 一种天然气轻烃回收的方法及装置
CN106350113A (zh) * 2015-07-15 2017-01-25 Ifp 新能源公司 用于处理烃进料的方法

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3544855A1 (de) * 1985-12-18 1987-06-19 Linde Ag Verfahren zur abtrennung von c(pfeil abwaerts)5(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)-kohlenwasserstoffen aus einem gasstrom
FR2615184B1 (fr) * 1987-05-15 1989-06-30 Elf Aquitaine Procede cryogenique de desulfuration selective et de degazolinage simultanes d'un melange gazeux consistant principalement en methane et renfermant egalement h2s ainsi que des hydrocarbures en c2 et plus
DE3802553C2 (de) * 1988-01-28 1996-06-20 Linde Ag Verfahren zur Abtrennung von Kohlenwasserstoffen
DE3814294A1 (de) * 1988-04-28 1989-11-09 Linde Ag Verfahren zur abtrennung von kohlenwasserstoffen
GB2224036B (en) * 1988-10-21 1992-06-24 Costain Eng Ltd Separation of gas & oil mixtures
FR2646166B1 (fr) * 1989-04-25 1991-08-16 Technip Cie Procede de recuperation d'hydrocarbures liquides dans une charge gazeuse et installation pour l'execution de ce procede
US5265427A (en) * 1992-06-26 1993-11-30 Exxon Production Research Company Refrigerant recovery scheme
US5390499A (en) * 1993-10-27 1995-02-21 Liquid Carbonic Corporation Process to increase natural gas methane content
DE19752703A1 (de) * 1997-11-27 1999-06-02 Linde Ag Verfahren und Anlage zum Abtrennen von C2- oder C2+-Kohlenwasserstoffen
US6329926B1 (en) * 1998-11-02 2001-12-11 Newport Electronics, Inc. Visual display devices
US6243021B1 (en) * 1998-11-02 2001-06-05 Newport Electronics, Inc. Indicating and measuring instrument
US20060260355A1 (en) * 2005-05-19 2006-11-23 Roberts Mark J Integrated NGL recovery and liquefied natural gas production
US20070130991A1 (en) * 2005-12-14 2007-06-14 Chevron U.S.A. Inc. Liquefaction of associated gas at moderate conditions
CA2656775C (en) * 2006-07-10 2011-06-14 Fluor Technologies Corporation Configurations and methods for rich gas conditioning for ngl recovery
US20080016910A1 (en) * 2006-07-21 2008-01-24 Adam Adrian Brostow Integrated NGL recovery in the production of liquefied natural gas
CN102977910B (zh) * 2011-09-02 2014-11-19 中国石油化工集团公司 一种轻烃回收***及方法
WO2017177317A1 (en) * 2016-04-11 2017-10-19 Geoff Rowe A system and method for liquefying production gas from a gas source

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3932156A (en) * 1972-10-02 1976-01-13 Hydrocarbon Research, Inc. Recovery of heavier hydrocarbons from natural gas
US4272269A (en) * 1979-11-23 1981-06-09 Fluor Corporation Cryogenic expander recovery process
IT1136894B (it) * 1981-07-07 1986-09-03 Snam Progetti Metodo per il recupero di condensati da una miscela gassosa di idrocarburi
US4597788A (en) * 1982-03-10 1986-07-01 Flexivol, Inc. Process for recovering ethane, propane and heavier hydrocarbons from a natural gas stream
US4584006A (en) * 1982-03-10 1986-04-22 Flexivol, Inc. Process for recovering propane and heavier hydrocarbons from a natural gas stream
DE3319986A1 (de) * 1983-06-01 1984-12-06 Linde Ag, 6200 Wiesbaden Verfahren zum abtrennen von c(pfeil abwaerts)2(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)-kohlenwasserstoffen aus erdgas
CA1235650A (en) * 1983-09-13 1988-04-26 Paul Kumman Parallel stream heat exchange for separation of ethane and higher hydrocarbons from a natural or refinery gas
US4507133A (en) * 1983-09-29 1985-03-26 Exxon Production Research Co. Process for LPG recovery
US4548629A (en) * 1983-10-11 1985-10-22 Exxon Production Research Co. Process for the liquefaction of natural gas
DE3408760A1 (de) * 1984-03-09 1985-09-12 Linde Ag, 6200 Wiesbaden Verfahren zur gewinnung von c(pfeil abwaerts)3(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)-kohlenwasserstoffen
DE3414749A1 (de) * 1984-04-18 1985-10-31 Linde Ag, 6200 Wiesbaden Verfahren zur abtrennung hoeherer kohlenwasserstoffe aus einem kohlenwasserstoffhaltigen rohgas
US4617039A (en) * 1984-11-19 1986-10-14 Pro-Quip Corporation Separating hydrocarbon gases
US4596588A (en) * 1985-04-12 1986-06-24 Gulsby Engineering Inc. Selected methods of reflux-hydrocarbon gas separation process

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101952003A (zh) * 2007-03-06 2011-01-19 林德股份公司 分离方法
CN106350113A (zh) * 2015-07-15 2017-01-25 Ifp 新能源公司 用于处理烃进料的方法
CN106350113B (zh) * 2015-07-15 2020-10-16 Ifp 新能源公司 用于处理烃进料的方法
CN105783421A (zh) * 2016-04-07 2016-07-20 成都赛普瑞兴科技有限公司 一种天然气轻烃回收的方法及装置

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