CN104769376B - 用于低温分离一氧化碳、甲烷及氢气和/或氮气的混合物的设备和方法 - Google Patents
用于低温分离一氧化碳、甲烷及氢气和/或氮气的混合物的设备和方法 Download PDFInfo
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Abstract
一种用于低温分离甲烷、一氧化碳和氢气的混合物(5)的设备,该设备包括:第一分离单元,该第一分离单元包括第一塔(19),第一分离单元被供给所述混合物(5);用于排放来自第一单元的富含氢气的气体(21)的第一管道;用于排放来自第一单元的含有甲烷和一氧化碳的液体(23)的第二管道;连接至第二管道的第二塔(27);连接至第二塔的贮槽以提取富含甲烷的液体(33)的第三管道;和连接至第二塔的塔顶以提取富含一氧化碳的气体(43)的第四管道,第一管道布置于第二塔下面,所述两个塔具有相同的主轴线,使得在比第二塔的贮槽的压力更高的压力下产生所述富含甲烷的液体(33)。
Description
技术领域
本发明涉及一种用于低温分离一氧化碳、甲烷和氢气以及可选地氮气的混合物的设备和方法。
所述混合物可以含有:
-一氧化碳、氢气,以及甲烷和氮气杂质(H2/CO冷箱);
-氮气及氢气、一氧化碳和甲烷杂质(用氮气清洗的冷箱)。
背景技术
已知对一氧化碳、氢气和甲烷的混合物进行第一次低温分离以产生富氢气体和主要含有CO、CH4(和氮)的液体混合物。该第二混合物通常在CO/CH4塔中分离以产生富含一氧化碳的气体(含氮)和富含甲烷的液体。
可以列举出用于进行第一次分离的若干种方法。
已知进行一氧化碳、氢气和甲烷的混合物的第一次分离,以便通过部分冷凝来去除氢气,随后在CO/CH4塔中对主要含有一氧化碳(与氮气)和甲烷的第二混合物进行第二次分离。
还已知的是,在一氧化碳或甲烷或氮洗涤塔中进行混合物的第一次分离以产生一氧化碳和甲烷的第二混合物。然后该第二混合物在CO/CH4塔中分离。
本发明的一个目的是当甲烷必须在压力下生产时使用于低温分离一氧化碳、氢和甲烷的混合物的设备更紧凑。
本发明的另一个目的是,在某些情况下降低用于低温分离一氧化碳、氢和甲烷的混合物的设备的最大高度。这降低了设备的成本以及运输成本。
在适当的情况下,从CO/CH4塔的底部抽出的液态甲烷可以在泵中被加压以便随后被储存和/或输送到客户,或者随后被送至甲烷洗涤塔的顶部。
本发明的另一个目的是向液态甲烷泵供给由通过使CO/CH4塔的底部的高度升高获得的静压力来加压的液体。
前序部分的特征从EP-A-1080765已知。
发明内容
根据本发明的一个主题,提供了一种用于低温分离甲烷、一氧化碳和氢气以及可选地氮气的混合物的设备,该设备包括:具有至少第一塔和/或相分离器的第一分离单元,所述第一分离单元被供给所述混合物;用于从第一单元排放富含氢气和可选地富含氮气的气体的第一管道;用于从第一塔或从相分离器排放含有甲烷和一氧化碳的液体的第二管道;连接至第二管道的第二塔,连接至第二塔的底部以抽取富含甲烷的液体的第三管道;和连接至第二塔的顶部以抽取富含一氧化碳或氮气的气体的第四管道,第一塔和/或一个或多个相分离器被定位于第二塔下面,该两个塔或第二塔和相分离器具有相同的主轴线,从而富含甲烷的液体在比第二塔的底部压力更高的压力下产生,第二塔包括底部再沸器,其特征在于,在适当情况下,当所述设备包括第一塔时,该设备不包括用于输送来自第一塔的塔顶气体以便加热第二塔的底部再沸器的装置,并且其中第二管道是连接至第一塔的底部的管道。
根据其它可选方面,所述设备包括:
-连接至第三管道的泵,该泵定位成比第二塔的底部更接近地面;
-辅助塔,该辅助塔的顶部可选地连接至泵,该辅助塔的底部通过用于将来自第一塔的塔顶气体送至辅助塔底部的装置和用于将来自辅助塔的底部液体送至第一塔的顶部的装置连接至第一塔的顶部,辅助塔紧邻第一塔定位;
-辅助塔定位成使其底部比第一塔的顶部离地面更远;
-辅助塔附接至第二塔;
-第一单元包括预处理塔、用于将混合物从预处理塔送至第一塔的管道,辅助塔附接至该预处理塔;
-所述设备包括处于第二塔下游的后处理塔,辅助塔附接至该后处理塔;
-第一单元包括甲烷洗涤塔,该塔连接至第一塔以便向其供给混合物,该混合物是来自甲烷洗涤塔的底部液体,甲烷洗涤塔的顶部连接至所述泵;
-第一单元包括相分离器和用于输送来自相分离器的液体例如供给第一塔的混合物的装置;
-第一单元包括洗涤塔和第一塔,洗涤液体富含一氧化碳,第一单元还包括用于将来自洗涤塔的底部液体送至第一塔的装置;
-第一单元包括洗涤塔,洗涤液体富含氮,所述洗涤塔构成第一塔;
-用于产生作为最终产品的液态甲烷的装置;
-第一单元包括氮洗涤塔,第二液体含有甲烷和氮以及第二塔产生富氮气体。
根据本发明的另一主题,提供了一种用于低温分离甲烷和一氧化碳以及氢气和可选地氮气的混合物的方法,其中,利用被供给混合物的至少第一塔或相分离器进行所述混合物的第一分离以在第一塔或相分离器的底部产生富含甲烷和含有一氧化碳和/或氮的流体,所述流体在第二塔中被分离以产生富含一氧化碳和可选地富含氮气的气体以及富含甲烷的液体,第一塔或相分离器定位于第二塔下面,所述两个塔或所述第二塔和相分离器具有相同的主轴线,从而富含甲烷的液体至少部分地通过静压力加压,所述第二塔包括底部再沸器,其特征在于,在适当情况下,所述底部再沸器通过不是来自第一塔的塔顶气体的气体加热,并且富含甲烷的流体源自第一塔的底部。
根据本发明的其它可选方面:
-所述底部再沸器通过循环气体加热,该循环气体是一氧化碳;
-来自第一塔的塔顶气体在交换器中被再加热,混合物在该交换器中被冷却;
-来自第一塔的全部塔顶气体在交换器中被再加热;
-所述富含甲烷的液体部分地通过定位成比第二塔的底部更接近地面的泵被加压;
-所述泵处于地面上;
-来自第一塔的塔顶气体被送至辅助塔的底部,富含甲烷的液体被送至所述塔的顶部,所述辅助塔定位成紧邻第一塔;
-第一单元包括预处理塔、用于将混合物从预处理塔送至第一塔的管道,辅助塔附接至该预处理塔;
-所述设备包括处于第二塔下游的后处理塔,所述辅助塔附接至所述后处理塔;
-第一单元包括甲烷洗涤塔,来自洗涤塔的底部液体作为混合物被送至所述第一塔,经加压的富含甲烷的液体被送至洗涤塔;
-第一单元包括洗涤塔,该洗涤塔被供给富含一氧化碳或氮的洗涤液体,来自洗涤塔的底部液体被送至第一塔;
-所述方法产生作为最终产品的液态甲烷,该产品源自第二塔的底部;
-第一单元包括氮洗涤塔,第二液体含有甲烷和氮,第二塔产生富氮气体。
附图说明
下面将参照附图更详细地说明本发明。
图1示出了根据现有技术的甲烷洗涤方法,图2和3示出了根据本发明的甲烷洗涤方法,图4示出了根据现有技术的部分冷凝方法,图5示出了根据本发明的部分冷凝方法,图6示出了根据现有技术的一氧化碳洗涤方法,图7示出了根据本发明的一氧化碳洗涤方法,图8示出了根据现有技术的氮洗涤方法,图9示出了根据本发明的氮洗涤方法。
具体实施方式
根据图1,氢气、一氧化碳和甲烷的混合物1在单元3中被净化以去除水和二氧化碳。经净化的混合物5在主低温交换器9中被冷却以便被送至相分离器7,在相分离器中被分离以形成富含氢气的气体11和富含甲烷的液体13。气体11在甲烷洗涤塔17中被分离,该甲烷洗涤塔在顶部被供给富含甲烷的洗涤液体41。
来自塔17的底部液体与液体13混合以形成富含CO和CH4并且还含有氮的液体18,该液体18被送至具有底部再沸器22的闪蒸塔19的顶部。在塔19的顶部抽取的气体21富含氢气并且在交换器9中被再加热以用于升级成通常送至燃料网络的吹扫气体。
来自塔19的底部液体23主要含有一氧化碳(和氮)和甲烷,并且在阀25中膨胀,然后被送至CO/CH4塔27中进行分离。富含一氧化碳的气体44在所述塔的顶部形成,富含甲烷的液体33在所述塔的底部形成。液体33被分成两部分,一个部分37在主低温交换器9中被再加热(或未再加热)以用于升级成CO/CH4塔的压力(几个巴)下的吹扫气体(或通过绕过交换器9而处于液态形式),另一部分35通过泵36被加压以供给甲烷洗涤塔17的顶部并用于可选地借助于主低温交换器9以气态形式在压力下升级(流体38)(或通过绕过交换器9而直接以液态形式升级)。
一氧化碳循环确保所述设备保持低温。源自塔27的顶部的一氧化碳在交换器9中被再加热,作为流45送至压缩机51。一部分一氧化碳在该压缩机的出口处生成为处于压力下的气体53。另一部分57在交换器9中被冷却并分成两部分。处于交换器9的中间温度的一部分59在涡轮61中膨胀并经由阀63通过管道65送至压缩机51。另一部分67继续在交换器9中被冷却。冷却的一氧化碳的一份69用于加热闪蒸塔19的底部再沸器22并且被冷凝。另一份71用于加热CO/CH4塔27的底部再沸器31并与冷凝的份69混合。整个流73在阀75中膨胀并被送至CO/CH4塔的塔顶冷凝器29,在该处气化以形成一氧化碳流43,该一氧化碳流43与来自CO/CH4塔的塔顶气体混合。
来自塔顶冷凝器29的液体77的一部分被送至相分离器79。从相分离器79抽取出液体81,该液体被送至交换器21,该交换器使来自甲烷洗涤塔的中间提取物冷却,液体81在该交换器中气化,所得的气体被送至相分离器79。来自相分离器79的气体83与气体43一起被送至压缩机51的入口。
应指出的是,三个塔17、27、19全部放置在地面上,这增加了占地面积(空间要求)。为了响应用于向泵36供给富含CH4的液体所需的静压高度而不发生气蚀的风险,塔27被升高至足够的高度。
根据本发明,如图2所示,CO/CH4塔27被安放在闪蒸塔19的上面,所述两个塔具有相同的主轴线。因此,来自所述塔27的底部的富含甲烷的液体33穿过高度H从而到达泵36并且由于静压力而处于较高压力下。可以使用该处于升高的压力下的液体的一部分作为泵36的下游或上游的产品。冷箱的所述塔的地面空间要求因此被降低。此外,如果两个塔27和19的高度的总和小于塔17的高度,则冷箱的塔的壳体长度不被改变。
在利用如图1所示的传统甲烷洗涤的冷箱中,来自洗涤塔17的底部的液相18被送至闪蒸塔19。这具有消除仍溶解在一氧化碳中的残余氢的作用。
与图1不同,为了改进一氧化碳的回收,闪蒸塔在塔的顶部包括数个附加的塔板,构成相对于塔19减小了直径的辅助塔20。在该附加部段,气相通过液态甲烷39以逆流方式被洗涤,从而从中萃取仍溶解的一氧化碳。在该部段20中的液体/蒸汽流动是非常低的:流入闪蒸塔19的其它全部气体流位于所述部段20的下面。为了确保良好的液体/蒸汽分布和各相之间好的接触而使闪蒸塔的上部部段20的直径减小:因此称为“辅助塔”(尖塔)。
塔19在辅助塔下面被供给洗涤液体18。辅助塔20在顶部被供给源自泵36的富含甲烷的液体39。来自辅助塔的塔顶气体21在交换器9中被再加热后作为吹扫气体送出。
(A)为了帮助其支承,辅助塔20在大约一米的长度上结合在闪蒸塔19中。
此外,由于CO/CH4塔27的安放要求特定高度以便能够向位于底部的甲烷泵或各泵36供给足够可用的净正吸入压头(标注为NPSH),在图2中,建议将CO/CH4塔27定位于闪蒸塔19(具有或不具有辅助塔20)的上方。这两个塔19、27或三个塔19、20、27的竖直累积常常组合在一起,其确定了塔的壳体的高度尺寸。然后图3示出了另一变型,使得能减小塔的壳体(闪蒸塔19与CO/CH4塔27的组件)的竖直尺寸。
本发明的一个创新包括从闪蒸塔的顶部重新定位辅助塔20,例如通过将其附接至洗涤塔17的侧面。该重新定位可以在冷箱的其它位置进行(例如在另一塔上,例如第二塔27或后处理塔如脱氮塔),只要辅助塔20保持定位成具有高于闪蒸塔19的较低部分的压头。该概念使得可以降低以下两者:
·由于上面提到的理由(A),降低闪蒸塔19的较低部分的外壳的长度;
·由于辅助塔20的重新定位,降低CO/CH4塔27的外壳的高度(同时确保新的高度保持与所述或多个甲烷泵所要求的NPSH兼容)。
当所述“塔”的外壳尺寸设置成高度为“闪蒸塔19+CO/CH4塔27”组件的高度时,则该高度被减小。
根据图4,氢气、一氧化碳和甲烷的混合物1在单元3中被净化以去除水和二氧化碳。经净化的混合物5在主低温交换器9中被冷却以便被送至相分离器7,在相分离器中被分离以形成富氢气体11和富含甲烷的液体13。该液体13被送至具有底部再沸器22的闪蒸塔19的顶部。从塔101的顶部提取的气体21富含氢和在交换器9中再加热以用于升级成通常送至燃料网络的吹扫气体。
来自塔19的底部液体23主要含有一氧化碳和甲烷并且被送至CO/CH4塔27进行分离。富含一氧化碳的气体在所述塔的顶部形成,富含甲烷的液体33在所述塔的底部形成。液体35在交换器中再加热以用作燃料。液体33被分成两部分,一个部分37在主低温交换器9中被再加热(或未再加热)以用于升级成CO/CH4塔的压力(几个巴)下的吹扫气体(或通过绕过交换器9而处于液态形式),另一部分35通过泵36被加压以用于可选地经由主低温交换器9以气态形式在压力下升级(流体38)(或通过绕过交换器9而直接以液态形式升级)。
一氧化碳循环确保所述设备保持低温。源自塔27的顶部的一氧化碳在交换器9中被再加热,作为流45送至压缩机51。一部分一氧化碳在压缩机的出口处生成为处于压力下的气体53。另一部分57在交换器9中被冷却并分成两部分。处于交换器9的中间温度下的一部分59在涡轮61中膨胀并经由阀63通过管道65送至压缩机51。另一部分67继续在交换器9中被冷却。冷却的一氧化碳的一份69用于加热塔19的底部再沸器22并且被冷凝。另一份71用于加热CO/CH4塔27的底部再沸器31并与冷凝的份69混合。整个流73在阀75中膨胀并被送至CO/CH4塔的塔顶冷凝器29,在该处气化以形成一氧化碳流43,该一氧化碳流43将在经过交换器9之后被送至压缩机51。
应注意的是,两个塔19和27都放置在地面上。
在图5的发明中,应注意的是,与图4不同,塔27定位于塔19的上方,塔19自身定位于相分离器7的上方。还可以将相分离器7放置成紧邻两个塔101、27。
根据图6,氢气、一氧化碳、氮气和甲烷的混合物1在单元3中被净化以去除水和二氧化碳。经净化的混合物5在交换器9中被冷却以便被送至相分离器7,在相分离器7处被分离以形成富含氢气的气体11和富含甲烷的液体13。气体11在一氧化碳洗涤塔601中被分离,该一氧化碳洗涤塔在顶部被供给富含一氧化碳的洗涤液体623。
来自塔601的底部液体与液体13混合以形成液体18,所形成的液体被送至具有底部再沸器22的闪蒸塔19的顶部。从塔19的顶部提取的气体21富含氢气并在交换器9中被再加热以用于升级成通常送至燃料网络的吹扫气体。
来自塔19的底部液体23主要含有一氧化碳和甲烷并且被送至CO/CH4塔27中进行分离。富含一氧化碳的气体43在所述塔的顶部形成,富含甲烷的液体33在所述塔的底部形成。液体33被分成两部分,一个部分37在主低温交换器9中被再加热(或未再加热)以用于升级成CO/CH4塔27的压力(几个巴)下的吹扫气体(或通过绕过交换器9而处于液态形式),另一部分35通过泵36被加压以用于可选地经由主低温交换器9以气态形式在压力下升级(流体38)(或通过绕过交换器9而直接以液态形式升级)。
一氧化碳循环确保所述设备保持低温。源自塔27的顶部的一氧化碳在交换器9中被再加热,作为流45送至压缩机51。一部分一氧化碳在压缩机的出口处生成为处于压力下的气体53。另一部分57在交换器9中被冷却并分成两部分。一部分59在阀63中膨胀然后通过管道65送至压缩机51。另一部分被分成两份。冷却的一氧化碳的一份69用于加热闪蒸塔19的底部再沸器22并且被冷凝。另一份71用于加热CO/CH4塔27的底部再沸器31并与冷凝的份71混合。整个流73在阀中膨胀并被送至CO/CH4塔的塔顶冷凝器619,在该处气化以形成一氧化碳流体43。塔27的顶部处的一氧化碳贮槽(bain)29向冷凝器619供给待冷凝的气体。
在一氧化碳含有过多氮气的情况下,来自塔27的塔顶气体635被送至具有塔顶冷凝器615的脱氮塔603。来自脱氮塔603的底部液体613在塔顶冷凝器615中被气化并与流体43混合以形成流体45,该流体45经由交换器9送至压缩机51。富含氮气的塔顶气体617在交换器9中被再加热并被送至燃料网络。在塔603中洗涤所需的一氧化碳由在压缩机51的排放部处提取的流体609和611提供。这些流体的一部分被作为流623送至洗涤塔601的顶部。当必须部分或全部地从所产生的气体中去除氮气时,上述所有情况都适用于安装脱氮塔。
应注意的是,四个塔601、19、27、603全部放置在地面上,这增加了占地面积。
根据图7的发明,CO/CH4塔27定位于闪蒸塔19上方,使得富含甲烷的液体流35在泵36的上游通过静压力加压。
图8示出了氮洗涤方法,其中氢气、一氧化碳、氮气和甲烷的混合物1离开单元804并且在净化单元3中被净化以去除水、甲醇和CO2(在上述所有情况中也可能要求吸附甲醇或在上游洗涤中使用的任何其他溶剂)。净化的混合物5在交换器9中被冷却然后送至相分离器7。来自相分离器7的气体与气体5的未冷却部分6混合以形成流11。流11的一部分用于再加热N2/CH4塔850的底部再沸器851,同时被部分冷凝。部分冷凝的流被送至相分离器809。来自分离器809的液体819富含甲烷并被送至泵36。来自分离器809的气体827与来自分离器7的气体821汇合,在交换器9中被冷却,然后在相分离器807中被分离,所产生的气体814供给至氮洗涤塔811以便被分离。
塔811在顶部被供给由气态氮流831在交换器9中的液化产生的液体流833。冷凝氮的另一部分835与来自塔811的含有氢气的经再加热的塔顶气体829混合并被送至CO2/H2S萃取单元(例如)804以用于热交换;所形成的气体843离开所述设备。
来自氮洗涤塔811的底部液体847膨胀,然后被送至相分离器845。所产生的气体853作为吹扫气体在交换器9中被再加热。液体849供给N2/CH4塔850以形成甲烷减少并富含氮气的气体流852和富含甲烷的液体流。富含甲烷的液体流35被送至泵36,然后供给相分离器821。气体825被送至交换器9以产生富含甲烷的气相。液体823可以也被送至交换器9以产生处于压力下的气态的富含甲烷的相,或者绕过交换器9以产生处于压力下的液态甲烷作为最终产品。还可以通过气化在泵36的上游取得的液体而产生低压下的气态或液态富含甲烷的相。
在图9的发明中,N2/CH4塔850定位于氮洗涤塔811上方。
还可以设想,通过独特地将塔27放置在相分离器上方——例如图4中的分离器7的上方、图6中的分离器7上方或图8中的分离器7、807、809、845中的一个的上方——而升高塔27。
Claims (23)
1.一种用于低温分离包含甲烷、一氧化碳和氢气的混合物(5)的设备,该设备包括:具有至少第一塔(19,811)和/或相分离器(7,807,809,821,845)的第一分离单元,所述第一分离单元被供给所述混合物(5,814);用于从第一单元排放富含氢气的气体(21,829)的第一管道;用于从第一塔或从相分离器排放含有甲烷和一氧化碳的液体(23,847,849)的第二管道;连接至第二管道的第二塔(27,850);连接至所述第二塔的底部以抽取富含甲烷的液体(33)的第三管道;和连接至第二塔的顶部以抽取富含一氧化碳或氮气的气体(43,852)的第四管道,所述第一塔和/或一个或多个相分离器被定位于第二塔下面,所述两个塔或所述第二塔和所述相分离器具有相同的主轴线,因此在比第二塔底部的压力更高的压力下产生富含甲烷的液体(33),第二塔包括底部再沸器(31),其特征在于,在适当情况下,所述设备不包括用于输送来自第一塔的塔顶气体以便加热第二塔的底部再沸器的装置,并且其中第二管道是连接至第一塔的底部的管道。
2.根据权利要求1所述的设备,包括连接至第三管道的泵(36),该泵定位成比第二塔(27,850)的底部更接近地面。
3.根据权利要求2所述的设备,包括辅助塔(20),该辅助塔的底部通过用于将来自第一塔的塔顶气体送至辅助塔底部的装置和用于将来自辅助塔的底部液体送至第一塔的顶部的装置连接至第一塔(19,811)的顶部。
4.根据权利要求3所述的设备,其中,所述辅助塔(20)定位成使其底部比第一塔(19)的顶部离地面更远。
5.根据权利要求3或4所述的设备,其中,所述辅助塔(20)附接至所述第二塔(27);或者所述第一单元包括预处理塔(17)、用于将混合物从预处理塔送至第一塔的管道,所述辅助塔附接至预处理塔;或者所述设备包括位于第二塔下游的后处理塔,所述辅助塔附接至后处理塔。
6.根据权利要求2至4中任一项所述的设备,其中,所述第一单元包括甲烷洗涤塔(17),该甲烷洗涤塔附接至第一塔(19)以便向第一塔供给混合物,该混合物是来自甲烷洗涤塔的底部液体,所述甲烷洗涤塔的顶部连接至所述泵(36)。
7.根据权利要求1至4中任一项所述的设备,其中,所述第一单元包括相分离器(7)和用于输送来自相分离器的液体的装置。
8.根据权利要求1至4中任一项所述的设备,其中,所述第一单元包括洗涤塔(601),洗涤液体富含一氧化碳,所述第一单元还包括用于将来自洗涤塔的底部液体送至第一塔(19)的装置。
9.根据权利要求1至4中任一项所述的设备,包括用于产生作为最终产品的液态甲烷的装置。
10.根据权利要求1所述的设备,其中,所述混合物包含甲烷、一氧化碳和氢气以及氮气。
11.根据权利要求10所述的设备,其中,所述第一管道用于从第一单元排放富含氢气和富含氮气的气体。
12.根据权利要求3所述的设备,其中,所述辅助塔的顶部连接至所述泵(36)。
13.根据权利要求3所述的设备,其中,所述辅助塔紧邻所述第一塔定位。
14.根据权利要求7所述的设备,其中,所述来自相分离器的液体是供给第一塔的混合物。
15.一种用于使用根据前述权利要求中任一项所述的设备低温分离包含甲烷和一氧化碳以及氢气的混合物的方法,其中,利用被供给所述混合物的至少第一塔(19,811)或至少相分离器(7,807,809,821,845)进行所述混合物的第一分离以产生富含甲烷并含有一氧化碳的流体(23,847,849),所述流体在第二塔(27,850)中被分离以产生富含一氧化碳的气体(45)以及富含甲烷的液体(35,37),第一塔或相分离器定位于第二塔下面,所述两个塔或所述第二塔与相分离器具有相同的主轴线,从而富含甲烷的液体至少部分地通过静压力加压,所述第二塔包括底部再沸器(31),其特征在于,在适当情况下,所述底部再沸器(31)通过来自第一塔的塔顶气体之外的气体(71)加热,并且富含甲烷的流体源自第一塔的底部。
16.根据权利要求15所述的方法,其中,所述底部再沸器(31)通过循环气体(71)加热,该循环气体是一氧化碳。
17.根据权利要求15或16所述的方法,其中,来自所述第一塔(19)的塔顶气体(21)在交换器(9)中被再加热,所述混合物在所述交换器(9)中被冷却。
18.根据权利要求17所述的方法,其中,来自所述第一塔的全部塔顶气体(21)在交换器(9)中被再加热。
19.根据权利要求15或16所述的方法,其中,所述富含甲烷的液体(35)部分地通过定位成比第二塔(27)的底部更接近地面的泵(36)被加压。
20.根据权利要求19所述的方法,其中,所述泵(36)位于地面上。
21.根据权利要求15所述的方法,其中,所述混合物包含甲烷和一氧化碳以及氢气和氮气。
22.根据权利要求21所述的方法,其中,所述混合物的所述第一分离产生富含甲烷并含有一氧化碳和氮的流体。
23.根据权利要求21所述的方法,其中,所述富含一氧化碳的气体(45)还富含氮气。
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