CN105934273A - 等离子体反应器与分解烃流体的方法 - Google Patents
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Abstract
在分解烃流体用的等离子体反应器(1)中,将减少或完全防止C颗粒的沉积。为了实现此目标,描述一种分解烃流体用的等离子体反应器(1),其包括:反应器腔室(2),其由反应器壁(3,3a)封闭且具有至少一个烃流体入口(5)以及至少一个出口(15);以及等离子体燃烧器(7),具有至少两个细长电极,其各自具有固定至反应器壁(3b)的底座部分(9)以及突出至反应器腔室(2)中且具有自由末端的燃烧器部分(11)。烃流体入口(5)展开至反应器腔室(2)中以使得自烃流体入口流出的烃流体沿着至少一个电极在反应器壁与电极之间的空间中流动至燃烧器部分的自由末端(12)。所述流体的高流率藉此得以实现,且进入的流体的流动方向被引导远离烃流体入口(5)。
Description
技术领域
本发明是关于分解烃流体用的等离子体反应器以及操作等离子体反应器的方法。
背景技术
图5描绘已知等离子体反应器1′,其在1990年代用作用于生产碳粒(或称为C颗粒)的测试反应器。现有等离子体反应器1′包括反应器腔室2′,其由具有下方部分3a′及盖3b′的反应器壁3′封闭。反应器腔室2′为实质上圆柱状的,且具有中心轴4′。多个烃流体入口5′设置于圆柱状外壁上,用于在径向方向上引导烃流体。包括细长电极(其未被详细展示)的等离子体燃烧器7′固定至反应器壁3′的盖3b′。等离子体燃烧器7′具有固定至反应器壁3′的盖3b′的底座部分9′。在与底座部分9′相对的等离子体燃烧器7′的另一末端处,等离子体燃烧器7′具有突出至反应器腔室2′中的燃烧器部分11′。在与等离子体燃烧器7′相对的反应器腔室2′的另一末端处,等离子体反应器1′具有出口15′,其中自进入的烃流体的裂解产生的物质可经由出口15′而逸出。在已知的等离子体反应器1′的操作中,等离子体13′形成于燃烧器部分11′的附近。烃流体是在朝向等离子体13′的方向上经由烃流体入口5′而引入。烃流体在不存在氧气的情况下且在高达2000℃的操作温度下分解为氢气及C颗粒,而氢气及C颗粒以H2/C气溶胶(aerosol)的形式自等离子体反应器的出口15′排出。
自US 5 481 080 A,已知一种等离子体燃烧器,其具有被配置为相互同轴的两个或超过两个管状电极。用于引入将由等离子体处理的气体的进气管同轴配置于内部管状电极内。进气管终止于会在系统操作时形成等离子体弧的两个管状电极的自由末端附近。
已知等离子体反应器会出现以下问题。在烃流体入口5′处存在碳沉积物的堆积,而碳沉积物一方面可能阻塞入口且另一方面可能导致不再可用于正产生的H2/C气溶胶的大块碳或C颗粒。为了防止烃在离开烃流体入口5′之后立即分解并因而导致沉积物,烃流体入口5′配置于相对于等离子体13′的足够大的距离d1处。此外,反应器壁3′由于高操作温度而必须远离等离子体13′而定位,以便减小反应器壁3′上的热负载。因此,反应器腔室2′必须为特定大小,如此导致在等离子体弧与反应器腔室的上方部分之间存在未使用的自由空间17′(参见图5)。热氢气尤其累积于自由空间17′中,且如此导致大量热损耗。此外,在此区域中存在大量热积聚,从而导致高达2500℃的温度。尤其由于不同的热膨胀系数以及因不同的热膨胀系数所致的材料中的应力,这些高温对电极以及反应器壁的材料造成实质性的需求。
发明内容
因此,本发明的目标为提供一种不产生或较少产生C颗粒的沉积物的等离子体反应器。此目标通过如权利要求1所述的等离子体反应器、如权利要求7所述的操作等离子体反应器的方法以及如权利要求10所述的用于生产合成烃的设施来实现。
本文所述的分解烃流体用的等离子体反应器包括:反应器腔室,其由反应器壁封闭且包括至少一个烃流体入口以及至少一个出口;以及等离子体燃烧器,包括至少两个细长电极,其各自具有固定至所述反应器壁的底座部分以及突出至所述反应器腔室中且具有自由末端的燃烧器部分。所述烃流体入口展开至所述反应器腔室中以使得自所述烃流体入口流出的烃流体沿着至少一个电极在所述反应器壁与所述电极之间的空间中流动至所述燃烧器部分的所述自由末端。通过烃流体入口的此种配置,可减少乃至完全防止C颗粒的沉积物,此是因为流体的高流率得以实现且进入的流体的流动方向被引导远离烃流体入口。
较佳地,所述烃流体入口与所述底座部分之间的距离小于所述烃流体入口与所述自由末端之间的距离。等离子体位于所述等离子体燃烧器的所述自由末端处且也产生辐射热。因为所述烃流体入口配置于所述底座部分附近,所以所述入口由所述等离子体燃烧器的本体屏蔽而免受辐射热。
有利地,所述等离子体燃烧器包括一个配置于另一个内的两个管状电极;且所述烃流体入口在径向方向上配置于外部管状电极外。在使用经久耐用的管状电极时,此种配置是有利的。
所述烃流体入口较佳经对准以使得自所述烃流体入口流出的所述烃流体在与所述电极的纵向范围相同的方向上流动。所述电极的过热以及所述反应器的上方区域中的热物质的累积藉此得以避免。流入的烃流体也充当反应器壁的热屏蔽。
较佳地,所述烃流体入口以及所述出口配置于所述反应器腔室的相对末端处。因此,在沿着所述等离子体燃烧器自所述烃流体入口至所述出口的方向上存在流动,且反应时间由于热区的改良的利用而减少。
有利地,所述烃流体入口具有冷却的入口通道以便降低C颗粒的沉积的可能性。
本文所述的根据实施例的操作等离子体反应器的方法实现前述目标在于,烃流体相对于反应器腔室的容积以500至10001/小时的空间速率穿过所述反应器腔室。高流率因此对抗C颗粒的沉积。
较佳地,在此方法中,沿着等离子体燃烧器自底座部分朝向自由末端而引导烃流体。电极的过热以及反应器的上方区域中的热物质的累积藉此得以避免。流入的烃流体也充当反应器壁的热屏蔽。
在所述方法中,有利地,以15至40巴、较佳18至22巴的压力引入烃流体。可压缩的气态氢形成于反应器腔室中。此外,若烃流体为气体(例如,天然气),则此气体也为可压缩的。可在前述压力下在反应器内实现较高密度的气态物质,藉此导致等离子体反应器的较高产量能力。因此,可在较高压力下使用较小反应器容积,藉此在制造及操作期间提供机械稳定的反应器容积及成本节省的优点。
上述等离子体反应器以及上述方法在用于生产合成烃的设施中提供优点,所述设施包括:根据上述实施例的等离子体反应器,用于将烃流体分解为碳及氢气;C转化器,用于实现(a)将碳与CO2转化为CO或(b)将碳与H2O转化为CO/H2气体混合物的制程,其中所述C转化器包括至少一个处理空间,其具有针对CO2或H2O的至少一个输入、至少一个气溶胶输入以及针对自所述转化制程产生的合成气体的至少一个C转化器输出。所述C转化器的所述气溶胶输入连接至所述等离子体反应器的输出。所述设施也包括CO转化器,其中所述CO转化器具有配置触媒的处理空间、用于自所述C转化器引入所述合成气体使之与所述触媒接触的其他构件以及用于将所述触媒和/或所述合成气体的温度控制或调节为预定温度的控制单元。在所述等离子体反应器、所述C转化器以及所述CO转化器中以15至40巴且尤其18至25巴的操作压力为主。因此可实现整个设施的高产量能力。此外,所述设施可直接附接至气体管线。
附图说明
在下文中,参看附图,通过较佳例示性实施例来描述本发明以及其他细节与优点。
图1为根据本揭露的分解烃流体用的等离子体反应器,其包括针对通过分解制程而获得的物质的输出。
图2为根据本揭露的分解烃流体用的等离子体反应器,其具有针对通过分解制程而获得的物质的多个输出。
图3为根据本揭露的等离子体反应器的烃流体入口。
图4为根据本揭露的使用等离子体反应器的用于生产合成烃的设施。
图5为根据现有技术的分解烃流体用的等离子体反应器。
具体实施方式
在下文描述中,术语“顶部”、“底部”、“右侧”及“左侧”以及类似术语相关于附图所示的定向及配置且仅欲描述实施例。这些术语可表示较佳配置,但不欲为限制性的。在本说明书的上下文中,术语“烃流体”意谓含有烃的流体(气体、气溶胶、液体)。
根据本揭露的等离子体反应器1包括反应器腔室2,其由具有下方部分3a及盖3b的反应器壁3封闭。反应器腔室2也可在除附图所示的位置之外的位置处划分。反应器腔室2为实质上圆柱状的,且具有中心轴4。具有细长电极(未详细展示)的等离子体燃烧器7固定至反应器壁3的盖3b。等离子体燃烧器7具有固定至反应器壁3(此处,特定言之,为盖3b)的底座部分9。在与底座部分9相对的等离子体燃烧器7的另一末端处,等离子体燃烧器7在电极的自由末端12处包括突出至反应器腔室2中的燃烧器部分11。可由等离子体控制元件14(例如,通过磁力)控制的等离子体13形成于电极之间。在与等离子体燃烧器7相对的反应器腔室2的另一末端处,等离子体反应器1具有出口15,其中自进入的烃流体的分解产生的物质可经由出口15而逸出。出口15在流动方向上配置于反应器腔室2的相对末端处。
此外,等离子体反应器1包括烃流体入口5,其配置于等离子体燃烧器7的底座部分9的附近。烃流体入口5展开至反应器腔室2中以使得自烃流体入口5流出的烃流体在朝向电极的自由末端的方向上流动至反应器壁3与等离子体燃烧器7的电极之间的自由空间17中。由于本文所述的等离子体燃烧器7的底座部分9的附近的烃流体入口5的配置,相对于等离子体13维持了足够间距d2(参见图1及图2)。即使反应器腔室2的内部较小(例如,在圆柱状反应器腔室的状况下,为较小直径),等离子体13与烃流体入口5之间的距离d2可仍大于现有技术中的等离子体反应器1′中的距离d1。可因此防止烃流体入口5处的C颗粒的沉积。烃流体入口5可如图3所说明而冷却。烃流体入口5具有由入口壁21围绕的入口孔19。入口壁21由冷却通道23围绕,且可充当反应器腔室2的热绝缘层。在操作中,冷却剂如箭头25所示流经冷却通道23。此外,烃流体如箭头27所示流经入口孔19。由于穿过其中而引导的冷却剂以及烃流体,烃流体入口5显著冷却至烃的分解温度以下,且C颗粒的沉积的可能性变得更小。
附图中未详细展示的电极较佳为管状电极或管式电极,所述电极其中一个配置于另一个内,诸如自US 5 481 080 A(参见上文)所知。在管式电极的状况下,进入的烃流体沿着电极(即,沿着外部电极)流动。在管式电极的状况下,烃流体入口5在径向方向上配置于外部管状电极外。然而,也可预想到使用两个棒式电极,例如,彼此靠近配置的两个棒式电极。在棒式电极的状况下,烃流体沿着两个或超过两个电极朝向其自由末端流动。因此,无论等离子体反应器1为何种类型,烃流体皆可在反应器腔室2与等离子体燃烧器7之间沿着至少一个电极流动至空间17中。
较佳将H2用作等离子体气体在电极之间形成等离子体弧13,此是因为H2在任何状况下皆自分解烃的制程产生。然而,任何其他适当气体可被选为等离子体气体,例如,诸如氩气或氮气的惰性气体,其中惰性气体不会在等离子体弧中影响或参与反应或裂解制程。
具有多个出口15的等离子体反应器1展示于图2中。第一出口15-1经设置以如同图1排出H2/C气溶胶。H2/C气溶胶的一部分可同样经由第二出口15-2而排出,此部分例如用于另一反应器或制程中。然而,较佳地,仅氢气H2经由第二出口15-2而排出,其中第二出口15-2是经设计以使得气态氢H2与固态C颗粒分开。
在等离子体反应器1操作时,等离子体13在燃烧器部分11的附近形成于电极之间。等离子体13通常具有介于600℃与2000℃之间的温度。烃流体(较佳为天然气)在不存在氧气的情况下在等离子体13的方向上经由烃流体入口5而被引导至反应器腔室2中。烃流体经引入以使得在操作中在反应器腔室2中达到高空间速率(单位为1/小时;与反应器腔室2的容积(立方米)相关的烃流体的流率(立方米/小时))。特定言之,考虑500至10001/小时的空间速率。由于引入的物质的高空间速率以及因此的高流率,额外减小在烃入口5上以及烃入口5附近沉积固体或C颗粒的威胁。
此外,反应器壁3与等离子体燃烧器7之间的自由空间17由流入的烃流体冷却。在等离子体反应器1的状况下,自由空间17可显著小于现有技术的等离子体反应器1′中的自由空间。因此,反应器腔室2可具有较小内部(在圆柱状反应器腔室2的状况下,为较小直径),藉此允许反应器腔室2具有较坚固的构造。坚固的反应器腔室2对于高操作压力是有利的。
由于本文所展示的烃流体入口5的配置,进入的烃流体的流动方向得以维持,此是因为出口15在流动方向上配置于反应器腔室2的相对末端处。因此,可能导致操作问题的自由空间17中的热物质的累积通过流入的烃流体而得以预防。此也减小污染的威胁,此是因为C颗粒通过流入的烃流体而被驱动向出口15。
烃流体一进入分解温度为主的接近等离子体13的区域,烃流体中所含有的烃便分解为C颗粒以及气态氢H2。分解温度取决于正引入的烃,且在例如天然气的状况下,大于600℃。氢气H2及C颗粒以H2/C气溶胶的形式自等离子体反应器的出口15排出。
有利地,到达烃流体入口的烃流体处于18至25巴的压力下。在此状况下,等离子体反应器1可直接连接至天然气管线,此是因为管线中的压力大致上处于此范围中。当系统操作时,同样在反应器腔室2中以约18至25巴的压力为主。在此压力下,诸如气态氢及天然气的气体成分(例如)经压缩以使得密度变高且产量可得以改良。
根据图2的等离子体反应器1的操作实际上与上文所述相同。仅有的差异在于氢气H2的一部分经由第二出口15-2移除。第二出口15-2经配置以使得C颗粒仅可困难地到达第二出口15-2或根本不到达第二出口15-2。此可(例如)通过曲径配置或通过配置第二出口15-2以使得其相对于烃流体或H2/C气溶胶的流动方向呈直角而实现。举例而言,第二出口15-2可相对于中心轴4且因此相对于总体流动方向以90°的角度配置(如图2所示)。第二出口15-2也可以与总体流动方向相反的角度配置,即,经定向以便在图2中向右上角倾斜。
图4展示用于生产合成烃的设施30,且包括如上所述的等离子体反应器1、用于(a)将碳与CO2转化为CO或(b)将碳与H2O转化为CO/H2气体混合物的C转化器32以及用于产生合成官能化和/或非官能化烃的CO转化器34。C转化器32包括至少一个处理空间,其具有针对CO2或H2O的至少一个输入、至少一个气溶胶输入以及针对自转化制程(a)或(b)产生的合成气体的至少一个C转化器输出。C转化器32的气溶胶输入连接至等离子体反应器1的输出15或15-1且接收H2/C气溶胶。C转化器32中的C颗粒的转化根据以下方程式中的任一个来实现:
(a)CO2+C→2CO或
(b)C+H2O→CO+H2。
通过来自H2/C气溶胶的H2,此导致由CO及H2组成的合成气体。举例而言,CO转化器34通过费雪-阙布希(Fischer-Tropsch)法(特定言之,通过SMDS法)来实施转化合成气体的制程。或者,通过柏吉斯-皮尔(Bergius-Pier)法、皮尔(Pier)法或皮尔法与MtL法(MtL=甲醇至液体)的组合来实现转化合成气体的制程。CO转化器34具有配置触媒的处理空间、用于自C转化器32引入合成气体使之与触媒接触的其他构件以及用于将触媒和/或合成气体的温度控制或调节为预定温度的控制单元。烃流体例如为天然气或类似气体,在设施30操作时,所述气体在无压力的任何改变的情况下以15至40巴且特定言之18至25巴的压力p1自(天然气)管线直接递送至等离子体反应器1。在等离子体反应器1的反应器腔室2中以相同压力p1为主。以相同压力(压力p2=p1)将自等离子体反应器1排出的H2/C气溶胶馈送至C转化器32中,且在850至1700℃的温度下与CO2或H2O混合以产生合成气体(CO及H2)。接着以相同压力(压力p3=p2=p1)将合成气体引入至CO转化器34中,且根据上述制程中的任一个而转化为合成烃。接着(以约1巴的较低环境压力p4)自设施移除合成烃。因此自等离子体反应器1直至CO转化器34以15至40巴(尤其为18至25巴)的实质上相同的操作压力为主。
可概括,可用本文所述的等离子体反应器1而实现以下优点:防止C颗粒的沉积物;利用等离子体13上方的反应器区域(自由空间17,其先前为热死容积(thermally dead volume));反应器的上方区域未过热,此是因为流入的烃流体使电极以及反应器壁冷却;流入的烃流体充当反应器壁3的热屏蔽;反应器腔室可由陶瓷(例如,Al2O3)制成;资本支出可降低;通过良好地利用由等离子体产生的热,电力消耗降低;反应器容积减小;沿着等离子体燃烧器7在自入口5至出口15的方向上引导流动的原理由于热区的改良的利用而减少反应时间。
已基于较佳例示性实施例来描述本发明,其中所描述的例示性实施例的个别特征可彼此自由地组合和/或可替换为另一个,只要所述特征是相容的。以相同方式,可省略所描述的例示性实施例的个别特征,只要所述特征并不是基本的。对于熟习此项技术的而言,许多修改及实施是可行且明显的,而不偏离本发明的范畴。
Claims (10)
1.一种分解烃流体用的等离子体反应器(1),包括:
反应器腔室(2),其由反应器壁(3、3a、3b)封闭且具有至少一个烃流体入口(5)以及至少一个出口(15、15-1、15-2);以及
等离子体燃烧器(7),具有至少两个细长的电极,所述电极各自包括固定至所述反应器壁(3、3a、3b)的底座部分(9)以及突出至所述反应器腔室(2)中且具有自由末端(12)的燃烧器部分(11);
其中所述烃流体入口(5)展开至所述反应器腔室(2)中以使得自所述烃流体入口(5)流出的烃流体沿着至少一个所述电极在所述反应器壁(3、3a、3b)与所述电极之间的空间(17)中流动至所述燃烧器部分(11)的所述自由末端(12)。
2.根据权利要求1所述的分解烃流体用的等离子体反应器(1),其中所述烃流体入口(5)与所述底座部分(9)之间的距离小于所述烃流体入口(5)与所述自由末端(12)之间的距离。
3.根据权利要求1或2所述的分解烃流体用的等离子体反应器(1),其中所述等离子体燃烧器(7)包括一个配置于另一个内的两个管状电极;且其中,所述烃流体入口(5)在径向方向上配置于外部管状电极外。
4.根据前述中任一项所述的分解烃流体用的等离子体反应器(1),其中所述烃流体入口(5)在所述电极的延伸方向上对准。
5.根据前述中任一项所述的分解烃流体用的等离子体反应器(1),其中所述烃流体入口(5)以及所述出口(15、15-1、15-2)配置于所述反应器腔室(2)的相对末端处。
6.根据前述中任一项所述的分解烃流体用的等离子体反应器(1),其中所述烃流体入口(5)包括冷却的入口通道(19)。
7.一种操作分解烃流体用的等离子体反应器的方法,所述分解烃流体用的等离子体反应器为如前述中任一项所述的分解烃流体用的等离子体反应器(1),其中相对于所述反应器腔室(2)的容积以500至10001/小时的空间速率将烃流体引导穿过所述反应器腔室(2)。
8.根据权利要求7所述的操作分解烃流体用的等离子体反应器的方法,其中沿着所述等离子体燃烧器(7)自所述底座部分(9)朝向所述自由末端(12)而引导所述烃流体。
9.根据权利要求7或8所述的操作分解烃流体用的等离子体反应器的方法,其中以18至22巴的压力将所述烃流体引入至所述反应器腔室(2)中。
10.一种用于生产合成烃的设施,包括:
如权利要求1至6中任一项所述的分解烃流体用的等离子体反应器(1),用于将烃流体分解为碳及氢气;
C转化器(32),用于实现(a)将碳与CO2转化为CO或(b)将碳与H2O转化为CO/H2气体混合物的制程,
其中所述C转化器(32)包括具有针对CO2或H2O的至少一个输入的至少一个处理空间、至少一个气溶胶输入以及针对自转化制程产生的合成气体的至少一个C转化器输出,其中所述C转化器(32)的所述气溶胶输入连接至所述等离子体反应器(1)的所述输出(15、15-1);以及
CO转化器(34),包括配置触媒的处理空间、用于自所述C转化器(32)引入所述合成气体使之与所述触媒接触的其他构件以及用于将所述触媒和/或所述合成气体的温度控制或调节为预定温度的控制单元;
其中在所述等离子体反应器(1)、所述C转化器(32)以及所述CO转化器(34)中以15至40巴且特定言之18至25巴的操作压力为主。
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DE102013020375.9A DE102013020375A1 (de) | 2013-12-06 | 2013-12-06 | Plasma-reaktor zum aufspalten eines kohlenwasserstoff-fluids |
DE102013020375.9 | 2013-12-06 | ||
PCT/EP2014/076737 WO2015082689A1 (en) | 2013-12-06 | 2014-12-05 | Plasma reactor and method for decomposing a hydrocarbon fluid |
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DE102013020375A1 (de) | 2015-06-11 |
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