CN102099648A - 用于富甲烷流的低温分离的方法和设备 - Google Patents

用于富甲烷流的低温分离的方法和设备 Download PDF

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CN102099648A
CN102099648A CN2008800201501A CN200880020150A CN102099648A CN 102099648 A CN102099648 A CN 102099648A CN 2008800201501 A CN2008800201501 A CN 2008800201501A CN 200880020150 A CN200880020150 A CN 200880020150A CN 102099648 A CN102099648 A CN 102099648A
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P·布里安
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及一种用于富甲烷原料流(1)的低温分离的方法，该富甲烷原料流还包含二氧化碳、氮和氧，该方法包括：将该流输送至吸附净化单元(3，29)用以生产相对于原料流贫含二氧化碳的流，将贫二氧化碳流的至少一部分冷却以便产生冷却流，将冷却流的至少一部分输送至蒸馏塔(17)，从蒸馏塔提取相对于原料流富含甲烷的流，从蒸馏塔提取相对于原料流富含氮和/或氧的流。脱二氧化碳罐通过受控的气态甲烷流再生。

Description

用于富甲烷流的低温分离的方法和设备
技术领域
本发明涉及一种用于富甲烷流的低温分离的方法和设备。
背景技术
为了净化来自有机源的富甲烷流以便生产净化的产品，需要去除例如二氧化碳、氧和氮的杂质。理想地，该产品包含低于2％的二氧化碳，且氧和氮的总的含量低于2％。
在本文中所有成分的百分比是摩尔百分比。
发明内容
根据本发明的一个目的，提供一种用于富甲烷原料流的低温分离的方法，该富甲烷原料流还包含二氧化碳以及氮或氧或氮和氧二者，在该方法中：
i)将该流输送至吸附净化单元以用于生产相对于原料流贫含二氧化碳的流；
ii)将贫二氧化碳流的至少一部分冷却以便产生冷却流；
iii)将冷却流的至少一部分输送至蒸馏塔；
iv)从该蒸馏塔提取相对于原料流富含甲烷的流；
v)从该蒸馏塔提取相对于原料流富含氮和/或氧的流；
vi)其特征在于，所述净化单元通过蒸发的富甲烷液体的至少一部分再生。
根据其它可选的特征：
-已经用作再生气体的蒸发的甲烷形成产品，且优选地包含1％至3％的二氧化碳；
-通过从所述塔提取的至少一种流体在所述塔的上游将贫二氧化碳流冷却；
-由所述塔中提取的流体是富氮流和/或富氧流；
-由所述塔中提取的流体是富甲烷流；
-富甲烷流以液体的形式提取；
-富甲烷液体通过与贫二氧化碳流热交换而蒸发；
-特别是通过和取自净化单元上游的蒸发的富甲烷液体的一部分混合，使已经用于再生的蒸发的液体的二氧化碳含量保持基本不变；
-至少部分地通过使来自外部源的液态氮流蒸发来维持冷却；
-液态氮通过与贫二氧化碳流热交换而蒸发；
-液态氮在所述塔的顶部的冷凝器中蒸发；
-至少部分地通过制冷循环维持冷却；
-以气态和/或液态形式生产富甲烷流；
-在需要时利用待分离的流的至少一部分加热所述塔的底部处的再沸器；
-从所述塔提取的富甲烷流包含至少98％甚至99％的甲烷；
-原料流包含75％至95％的甲烷；
-原料流包含的氮和/或氧的总量在3％至25％之间。
根据本发明的其它特征，提供一种用于富甲烷原料流的低温分离的设备，该富甲烷原料流还包含二氧化碳以及氮或氧或氮和氧二者，该设备包括：
i)吸附净化单元和用于向该吸附净化单元输送原料流以便产生相对于原料流贫含二氧化碳的流的装置；
ii)用于冷却贫二氧化碳流的至少一部分以便产生冷却流的装置；
iii)蒸馏塔和用于将冷却流的至少一部分输送至蒸馏塔的装置；
iv)用于从蒸馏塔提取相对于原料流富含甲烷的流的装置；以及
v)用于从蒸馏塔提取相对于原料流富含氮和/或氧的流的装置。
附图说明
下面结合附图更详细地描述本发明，其中图1和图6示意性地示出根据本发明的设备，图2是表示在根据本发明的设备的交换器中发生的热交换的图，图3和图4示出用于产生负大卡(frigories)的循环，该负大卡可用于产生根据本发明的方法所需的冷量，且图5示意性地示出根据本发明的设备的一个特征。
具体实施方式
在图1中，已经在渗透和/或吸附单元中净化过的处于环境温度和中等压力(5至15bar)的原料气体1包含＞75％的甲烷，＜2％的二氧化碳，以及总量＜25％的氧和氮。在这25％中，大约20％是氮，剩余的是氧。氧和氮的含量远远超出产品的要求。
气体1被输送至包括两个吸附剂罐3、29的吸附单元以便产生贫CO2流5。此流5被送至包含热交换器9、13和塔17的冷箱7。根据图2的图线，包含75％至95％的甲烷以及总量为3％至25％的氮和氧的流5在热交换器9中冷却且部分液化。
交换器9是铝或不锈钢钎焊板式交换器。
冷却的流5(其为两相流)确保塔17的底部再沸器11的再沸腾，产生的热23被传递至所述塔的底部。然后流5在热交换器13中液化，在阀15中膨胀至其压力的一半，并输送至塔17的中部。
在这个包含规整填料的塔17中进行液化流5的蒸馏，使得在底部产生富甲烷的液体流27，该液体流27包含总量小于2％的氮和氧，在所述塔的顶部产生气态流19，该气态流富含氮和/或氧，且包含小于5％的甲烷。
通过各种方法冷却塔17的顶部冷凝器67(图3和图4)，从而从所述塔去除热21。
例如，可通过使得来自外部源的液态氮缓慢流入而冷却冷凝器67。也可通过例如斯特林(Stirling)马达、Gifford MacMahon(G-M)机、脉冲管等的用于制冷的机器提供冷量。
可替代地，如图3所示，可由氮循环提供用于冷凝器67的负大卡。氮66被送至冷凝器67，在该冷凝器67处氮66蒸发形成气体67。气体67和来自分相器65的顶部的气体66混合，然后和流71混合。通过这种方法形成的流45被送至混合器，在交换器61、53中冷却，然后在压缩机44中压缩，该压缩机被供应有动力43。压缩流47在交换器49中冷却以形成流51，该流51在交换器53中被加热以便形成气体55并在涡轮机55中膨胀。流55被分成两个部分，一部分59被送至涡轮机69以便形成流71，剩余的部分57被送至交换器61。流57在阀63中膨胀并被送至分相器65。来自分相器65的液态流被送至冷凝器67。
另一可能性(图4)是使用布雷顿(Brayton)循环，该布雷顿循环使用氦作为循环流体。在冷凝器67中加热的气体81被送至交换器83，并在供应有动力87的压缩机85中压缩以便形成流89。此流被送至交换器91且然后送至交换器83。然后，此流被送至冷凝器67前在涡轮机93中膨胀。
在仅生产气体形式的甲烷的情况下，包含＜2％氮+氧和＞98％甲烷的液态甲烷27通过在交换器9中进行热交换而蒸发。
富含氮和/或氧的剩余物19在交换器13中将待分离的混合物复热，在交换器9中复热并被送至空气中。该剩余物包含小于5％的甲烷。
如图5中详细示出的，在交换器9中蒸发的甲烷被送至另一吸附剂罐29中从而使其再生，通过这种方法产生的再生气体32用作工艺/过程产品，该产品相对于流27富含二氧化碳，例如包含1％至3mol％之间的二氧化碳。
产品32的二氧化碳含量通过AIC分析器105进行分析，且通过阀103保持该含量基本不变，该阀103由AIC控制，该AIC开通一旁路通道101，该旁路通道根据要求使更加富含甲烷的气体102和流32混合。由于吸附器是循环操作的，需要这样的布置以便防止产品32的纯度的周期性变化。
可选地，如图1所示，产品32在一个或多个压缩机31中压缩至高压(20至30bar)且甚至是很高的压力(200至350bar)。
此产品包含稍高于＞96％甲烷，＜2％氮+氧，和＜2％CO2。
图6示出根据本发明的方法，该方法能够生产液体形式的甲烷。已经在渗透单元中净化过的原料气体1包含76.5％的甲烷，1.6％的二氧化碳，以及总量为22％的氧和氮。氧和氮的含量远远超出产品的要求。
气体1被输送至包括两个吸附剂罐3、29的吸附单元以便产生贫CO2流5。此流5被送至包含热交换器9、13和塔17的冷箱7。根据图2所示的图线，包含75％至95％的甲烷以及总量为3％至25％的氮和氧的流5在热交换器9中冷却且部分液化。
冷却的流5(其为两相流)确保塔17的底部再沸器11的再沸腾，产生的热23被传递至所述塔的底部。然后流5在热交换器13中液化，在阀15中膨胀并输送至塔17的中部。
液化流5在包含规整填料的塔17中蒸馏，从而在底部产生富甲烷的液体流27，该液体流27包含的氮+氧的总量小于2％，且在所述塔的顶部产生气态流19，该气态流富含氮+氧，且包含小于5％的甲烷。
通过使得来自外部源的液态氮201缓慢流入来冷却所述塔17的顶部冷凝器203(图3和4)。
富含氮和/或氧的剩余物19在阀25中膨胀，和缓慢流入的已蒸发的液态氮204混合，混合流207在混合器中混合，在交换器13中冷却待分离的混合物，在交换器9中被复热并被送至空气中。该剩余物包含小于5％的甲烷。
液态甲烷27被生产作为最终产品。
为了保持交换器9较冷，另一股缓慢流入的氮流211被送至交换器9，该氮流在该交换器9中蒸发形成流213。然后，此氮流213在作为流217排放至大气前用于使吸附剂罐215再生。
可替代地，如图1所示，氮211可由产品27的一部分代替。
应当理解，图1中示出的任何冷源可用于图6的方法。

Claims (16)

1.一种用于富甲烷原料流的低温分离的方法，该富甲烷原料流还包含二氧化碳以及氮或氧或氮和氧，在该方法中：
i)将该流输送至吸附净化单元(3，29)用以生产相对于原料流贫含二氧化碳的流；
ii)将该贫二氧化碳流的至少一部分冷却以便产生冷却流；
iii)将该冷却流的至少一部分输送至蒸馏塔(17)；
iv)从该蒸馏塔提取相对于原料流富含甲烷的流(27)；
v)从该蒸馏塔提取相对于原料流富含氮和/或氧的流(19)；其特征在于，
vi)利用蒸发的富甲烷液体的至少一部分使所述净化单元(3，29)再生。
2.根据权利要求1所述的方法，其特征在于，通过从所述塔(17)提取的至少一种流体在所述塔的上游将所述贫二氧化碳流冷却。
3.根据权利要求2所述的方法，其特征在于，所述从所述塔(17)提取的流体是所述富含氮和/或氧的流(19)。
4.根据权利要求2或3所述的方法，其特征在于，所述从所述塔(17)提取的流体是所述富甲烷流(27)。
5.根据权利要求4所述的方法，其特征在于，以液体的形式提取所述富甲烷流(27)。
6.根据权利要求5所述的方法，其特征在于，通过与所述贫二氧化碳流(5)热交换使所述富甲烷液体(27)蒸发。
7.根据前述权利要求之一所述的方法，其特征在于，特别是通过和取自所述净化单元上游的蒸发的富甲烷液体(101)的一部分混合，使已经用于再生的蒸发的液体的二氧化碳含量保持基本不变。
8.根据前述权利要求之一所述的方法，其特征在于，至少部分地通过使来自外部源的液态氮流(201，211)蒸发来维持冷却。
9.根据权利要求9所述的方法，其特征在于，液态氮通过与所述贫二氧化碳流热交换而蒸发。
10.根据权利要求8或9所述的方法，其特征在于，液态氮在所述塔(17)的顶部冷凝器(67)中蒸发。
11.根据前述权利要求之一所述的方法，其特征在于，至少部分地通过制冷循环维持冷却。
12.根据前述权利要求之一所述的方法，其特征在于，以气态和/或液态形式生产所述富甲烷流(27)。
13.根据前述权利要求之一所述的方法，其特征在于，在需要时利用待分离的流的至少一部分加热所述塔(17)的底部再沸器(11)。
14.根据前述权利要求之一所述的方法，其特征在于，从所述塔提取的所述富甲烷流包含至少98％的甲烷，或甚至99％的甲烷。
15.根据前述权利要求之一所述的方法，其特征在于，所述原料流(1)包含75％至95％的甲烷。
16.根据权利要求17所述的方法，其特征在于，所述原料流(1)包含总量在3％至25％之间的氮和/或氧。
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Application publication date: 20110615