CN1483133A - 针对紧凑型燃料处理器开车而加热催化剂的装置和方法 - Google Patents

针对紧凑型燃料处理器开车而加热催化剂的装置和方法 Download PDF

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CN1483133A
CN1483133A CNA01821276XA CN01821276A CN1483133A CN 1483133 A CN1483133 A CN 1483133A CN A01821276X A CNA01821276X A CN A01821276XA CN 01821276 A CN01821276 A CN 01821276A CN 1483133 A CN1483133 A CN 1483133A
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catalyst
catalyst bed
heating element
electrical heating
temperature
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CN100368753C (zh
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P
P·马丁
T·G·斯科特
J·L·潘
ʷ
J·F·史蒂文斯
C·克劳斯
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Texaco Development Corp
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Texaco Development Corp
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Abstract

为开车而加热催化剂床层(410)以及在过渡操作过程中为保持所希望的反应温度而为催化剂床层(410)供热的方法和装置。电加热元件(400)可以直接或间接加热所述催化剂。直接加热催化剂通过使加热器元件(400)与催化剂直接接触来实现。间接加热通过直接加热流体如工艺物流，而所述工艺物流反过来流过催化剂从而将热量传递给催化剂来实现。另外，间接加热可以通过将加热元件(400)放置在套内，而所述套随后与催化剂或流过催化剂的流体直接接触来实现。通过这些方式，多种形式的催化剂都可以应用这种催化剂加热器(400)，包括丸、挤出物、球以及整料。本发明的催化剂加热器(400)可以由任何电阻丝、释热元件或棒材制成，且所述加热器可以与电源偶合，从而提供能量进而产生热量。

Description

针对紧凑型燃料处理器 开车而加热催化剂的装置和方法
                       发明背景
燃料电池通过化学氧化还原反应供电，并且从清洁和效率角度来讲与其它发电形式相比拥有明显的优点。通常，燃料电池应用氢作燃料且用氧作氧化剂。发电量与反应物的消耗速率成正比。
阻止燃料电池更广泛应用的明显缺点是缺乏广泛分布的氢基本设施。氢具有相对低的体积能量密度，并且比目前在大多数发电系统中应用的烃燃料更难贮存和输送。克服这种困难的一种方法是应用重整器将烃转化为富氢气流，而后者可以用作燃料电池的进料。
烃基燃料如天然气、LPG、汽油以及柴油，均需要转化过程以用作大多数燃料电池的燃料源。现有技术应用了组合初始转化过程及几个纯化过程的多步方法。初始过程是最常用的蒸汽重整(SR)、自热重整(ATR)、催化部分氧化(CPOX)或非催化部分氧化(POX)。纯化过程通常包括脱硫、高温水-气变换、低温水-气变换、选择性CO氧化、或选择性CO甲烷化的组合。其它过程包括氢的选择性膜反应器和过滤器。
尽管已经有上述工作，但仍需要一种简单的装置将烃燃料转化为用于燃料电池的富氢气流。对于该问题任何解决方案所面临的实际困难是启动催化剂床层并在过渡操作过程中保持所希望的反应温度。本发明致力于满足这一需要。
发明概述
本发明具体涉及为开车而加热催化剂床层以及在过渡操作过程中为保持所希望的反应温度而为催化剂床层供热的方法和装置。这种方法和装置可以用于燃料处理器中，从而使燃料处理器的开车更加快速和容易。在燃料处理器中有几种催化剂可用于本发明，包括自热重整催化剂、部分氧化催化剂、蒸汽重整催化剂、水气变换催化剂、优先氧化催化剂和硫吸收剂，以及与邻接的燃料电池相连的阳极尾气氧化催化剂，但不局限于此。
作为本发明的实施方案，电加热元件可以直接或间接加热催化剂，从而在催化剂床层内迅速达到所希望的反应温度。直接加热催化剂通过使加热器元件与催化剂直接接触来实现。间接加热通过直接加热流体如工艺物流，而所述工艺物流反过来流过催化剂从而将热量传递给催化剂来实现。另外，间接加热可以通过将加热元件放置在套内，而所述套随后与催化剂或流过催化剂的流体直接接触来实现。如本发明范围所涉及的，多种形式的催化剂都可以应用催化剂加热器，包括丸、挤出物、球以及整料。在本发明的一种描述性实施方案中，本发明的催化剂加热器可以由任何电阻丝、释热元件(cartridge)或棒材制成，所述催化剂加热器可以如下文所述形成。能源如电源提供能量进而产生预热催化剂床层的热量。
本发明的一个描述性实施方案为一个在燃料处理器中的反应器，其中包括催化剂床层、设置在催化剂床层内的用于除去正常操作中过量热量的冷却盘管、以及设置在冷却盘管内的用于在开车或过渡操作中将催化剂加热到所希望的反应温度的电加热元件。这个优选的以及描述性的实施例在本发明中通常称之为套式加热。该描述性实施方案的重要的描述性优点包括：为快速和有效开车而为催化剂供热，预热加入燃料处理器的烃燃料原料，并且为在过渡操作过程中有助于反应器保持反应温度。
附图的简要描述
参照附图进行描述，其中：
图1描述了燃料处理器的流程简图。
图2描述了紧凑型燃料处理器。
图3描述了用于催化剂床层的表面加热器的一个描述性实施方案。
图4描述了利用电加热元件迂回穿过(weaving)整料型催化剂床层的一个描述性实施方案。
图5描述了利用电加热元件缠绕整料型催化剂床层的一个描述性
实施方案。
描述性实施方案的说明
本发明主要涉及为开车而加热催化剂床层以及在过渡操作过程中为保持所希望的反应温度而为催化剂床层供热的装置和方法。在一个优选方面，这里所描述的装置和方法涉及对紧凑型燃料处理器中的催化剂床层供热，而所述燃料处理器用于由烃燃料进料产生富氢气流。由这种紧凑型燃料处理器产生的富氢气体在燃料电池的发展中将会越来越重要，所述燃料电池包括用于电动车辆的燃料电池。但对于这里所描述的装置和方法来说，也预期存在其它可能的用途，包括不用于燃料处理器的放热催化剂床层的开车和保持反应温度。相应地，尽管在这里本发明是针对用于紧凑型燃料处理器和燃料电池而进行描述的，但是本发明的范围并不局限于该用途。
本发明的每一个描述性实施方案均涉及与燃料处理器相关的放热催化剂床层，其中烃燃料进料被引导通过所述燃料处理器。在环境温度下烃燃料可以是液体或气体，只要它能够被蒸发即可。在这里所使用的术语“烃”包括含有C-H键的有机化合物，所述化合物能够通过部分氧化或蒸汽重整反应产生氢。并不排除在化合物的分子结构中存在有不同于碳和氢的其它原子。这样，适用于这里所公开的方法和装置的燃料包括烃燃料如天然气、甲烷、乙烷、丙烷、丁烷、石脑油、汽油和柴油燃料、以及醇如甲醇、乙醇、丙醇等，但不局限于此。
燃料处理器的进料包括烃燃料、氧和水。氧可以为空气、富集空气或基本纯氧的形式。水可以以液体或蒸汽引入。进料组分的组成百分比由所希望的操作条件来确定，这将在下文中讨论。
燃料处理器流出物流包括氢和二氧化碳，并且也可以包括一些水、未转化的烃、一氧化碳、杂质(例如硫化氢和氨)、以及惰性组分(例如氮和氩，特别当空气作为进料物流的组分时)。
图1描述了燃料处理器的的基本流程图。本领域的熟练技术人员应该意识到在通过这里所公开的反应器的反应物流中需要一定量的累积量级(progressive order)。
步骤A是一个自热重整过程，其中两种反应，即部分氧化(下面通式I)和任选的蒸汽重整(下面通式II)组合进行，将进料物流F转化为含有氢和一氧化碳的合成气。通式I和II是例举性反应通式，其中将甲烷当作烃：
    (I)
      (II)
部分氧化反应发生得非常快，从而完全转化所加的氧并生成热。蒸汽重整反应发生得慢一些并消耗热。在进料物流中氧浓度较高有利于部分氧化反应，而水蒸汽浓度较高有利于蒸汽重整。因此，氧对烃的比率和水对烃的比率成为一个特征参数。这些比率影响操作温度和氢的收率。
根据进料条件和催化剂，自热重整步骤的操作温度范围可以为约550℃至约900℃。本发明应用包含或不包含蒸汽重整催化剂的部分氧化催化剂的催化剂床层。所述催化剂可以为任何形式，包括丸、球、挤出物、整料等。对本领域熟练技术人员来说，部分氧化催化剂应该是公知的，并且经常包括贵金属如在整料、挤出物、丸或其它载体上的氧化铝修补基面涂层(washcoat)上的铂、钯、铑和/或钌。非贵金属如镍或钴也已经被应用。其它修补基面涂层如二氧化钛、氧化锆、二氧化硅和氧化镁已经在文献中引述。在文献中许多附加材料如镧、铈和钾作为“助催化剂”被引述，其能改善部分氧化催化剂的性能。
对本领域熟练技术人员来说，蒸汽重整催化剂应该是已知的，并且可以包括镍及一定量钴或贵金属如铂、钯、铑、钌和/或铱。催化剂可以载带在氧化镁、氧化铝、二氧化硅、氧化锆或铝酸镁上，这些载体单独或组合应用。另外，蒸汽重整催化剂可以包括镍，优选载带在氧化镁、氧化铝、二氧化硅、氧化锆或铝酸镁上，并利用碱金属如钾进行促进，其中这些载体单独或组合应用。
过程步骤B是冷却步骤，用于将来自过程步骤A的合成气流冷却到约200℃至约600℃的温度，优选为约300℃至约500℃，并且更优选为约375℃至约425℃，从而优化去下一步的合成气流出物的温度。这一冷却可以依据设计规范和回收/循环气流热量的需要通过受热器(heat sink)、热管或换热器来实现。步骤B的一个描述性实施方案是应用换热器，该换热器应用进料物流F作为循环通过换热器的冷却剂。该换热器可以应用本领域熟练技术人员已知的任何适当结构，包括管壳式、板式、盘管式等。另外或附加的是，冷却步骤B可以伴随着注入附加的进料组分如燃料、空气或水。水是优选的，因为当其蒸发为蒸汽时能够吸收大量的热。所加组分的量取决于所希望的冷却程度，并且可以很容易地由本领域技术人员确定。
过程步骤C是纯化步骤。烃物流的一种主要杂质是硫，其通过自热重整步骤A转化为硫化氢。用于过程步骤C的处理核心优选包括能够吸收和转化硫化氢的氧化锌和/或其它材料，并且可以包括载体(例如整料、挤出物、丸等)。脱硫是按照下列反应通式III将硫化氢转化成水完成的：
    (III)
其它杂质如氯化物也可以被脱除。所述反应优选在约300℃至约500℃的温度下进行，更优选为约375℃至约425℃。氧化锌在约25℃至约700℃的宽温度范围内均是有效的硫化氢吸收剂，并且通过适当选择操作温度对于优选过程步骤的顺序来说具有很大的灵活性。
然后可以将流出物流送入混合步骤D，其中任选向气流中加入水。水的加入使得当其蒸发时降低了反应物流的温度，并且为过程步骤E(在下文讨论)的水气变换反应提供更多的水。水蒸汽和其它流出物流组分通过流过惰性材料如陶瓷球或其它类似材料的处理核心进行混合，这些惰性材料有效混合和/或有助于水的蒸发。另外，任何附加的水都可以与进料一起引入，并且可以重新安排混合步骤，从而为下面公开的CO氧化步骤G提供更好的氧化气体的混合。
过程步骤E为水气变换反应，其按照通式IV将一氧化碳转化为二氧化碳：
    (IV)
这是一个重要步骤，因为一氧化碳除了对人具有高毒性外，对燃料电池也是一种毒物。一氧化碳的浓度应该优选降低到能够被燃料电池忍受的水平，通常低于50ppm。根据所应用的催化剂，通常水气变换反应可以在温度为150℃-600℃下发生。在这种条件下，气流中的大部分一氧化碳在这一步中转化。
低温变换催化剂在约150℃至约300℃的范围内操作，并且包括例如氧化铜、或载带在其它过渡金属氧化物如氧化锆上的铜、载带在过渡金属氧化物或耐火载体如二氧化硅、氧化铝、氧化锆等上的锌、或在适当载体如二氧化硅、氧化铝、氧化锆等上的贵金属如铂、铼、钯、铑或金。
高温变换催化剂优选在约300℃至约600℃的温度范围内操作，并且可以包括过渡金属氧化物如氧化铁或三氧化二铬，并且任选包括一种助催化剂如铜或铁的硅化物。高温变换催化剂还包括载带的贵金属如载带的铂、钯和/或其它铂族元素。
用于进行这一步骤的处理核心可以包括如上面描述的高温或低温变换催化剂的填充床、或者高温和低温变换催化剂的组合。所述过程应该在任何适合水气变换反应的温度下操作，依据所用催化剂的类型，优选在150℃至约400℃的温度下操作。任选地，冷却元件如冷却盘管可以设置在变换反应器的处理核心中，从而降低在催化剂填充床层内的反应温度。较低的温度有利于一氧化碳转化为二氧化碳。另外，通过利用在高温和低温变换步骤之间的脱硫组件提供独立的高温和低温变换步骤，可以在高和低的变换转化率之间进行纯化处理步骤C。
过程步骤F是在一种描述性实施方案中利用换热器进行的冷却步骤。所述换热器可以为任何适当结构，包括管板式、板式和盘管式等。另外也可以应用热管或其它形式的受热器。换热器的目的是降低气流温度，从而产生温度范围优选为约90℃至约150℃的流出物。
向步骤F的过程中加入氧。所述氧由下面描述的过程步骤G的反应消耗。所述氧可以为空气、富集空气、或基本上纯氧的形式。换热器可以通过设计提供空气与富氢气体的混合。另外，过程步骤D的描述性实施方案可以用于进行混合。
过程步骤G是氧化步骤，其中在流出物流中几乎全部剩余的一氧化碳均被转化为二氧化碳。所述处理在一氧化碳氧化催化剂存在时进行，并且所述催化剂可以为任何适当的形式如丸、球、整料等。一氧化碳氧化催化剂是已知的，并且通常包括贵金属(例如铂、钯)和/或过渡金属(如铁、铬、锰)、和/或贵金属或过渡金属的化合物，具体为氧化物。优选的氧化催化剂为氧化铝修补基面涂层上的铂。所述修补基面涂层可以被涂到整料、挤出物、丸或其它载体上。可以加入附加材料如铈或镧以改善性能。在文献中已经引述了许多其它配方，同时某些实施者宣称铑或氧化铝催化剂有优越的性能。钌、钯、金以及其它材料在文献中也作为此用途的活性物质而被引述。
在过程步骤G中发生两个反应：所希望的一氧化碳氧化(通式V)和不希望的氢氧化(通式VI)，如下所示：
      (V)
    (VI)
低温有利于优先氧化一氧化碳。因为两个反应都产生热，有利的是任选包括一个冷却元件，如设置在过程内的冷却盘管。所述过程的操作温度优选保持在约90℃至约150℃的范围内。过程步骤G优选降低一氧化碳的含量至低于50ppm，该含量适合用于燃料电池，但是本领域的熟练技术人员应该意识到本发明可以用于产生一氧化碳含量更高和更低的富氢产品。
流出燃料处理器的流出物为含有二氧化碳和其它组分的富氢气体，其中可以存在的如水、惰性组分(例如氮、氩)、残余烃等。产品气体可以用作燃料电池的进料或用于其中需要富氢进料物流的其它用途。任选地，可以将产品气体送到进一步的处理过程中，以脱去二氧化碳、水或其它组分。
在燃料处理器的一个描述性实施方案中，紧凑型燃料处理器为具有单独的组件单元的组件结构，这些组件单元是可拆卸、可重装并且可单独更换。参照图2，紧凑型燃料处理器100包括一系列独立组件(110、120、130、140、150、160和170)。所述组件单元可以用于任何取向，如垂直或水平取向，并且适合与燃料电池组合应用，从而将这里描述的反应器的富氢产品气体作为进料物流直接供给燃料电池。尽管所述组件可以具有任何横截面结构，如圆形、矩形、三角形等，但圆形横截面对通常为管状的燃料处理器100来说是优选的。
图2所示的燃料处理器100实现了图1中所示的过程。进料物流F通过入口管102引入，产品气体P通过出口管103采出。所述装置100包括几个可以堆放形成组件组的组件，所述组件组可以通过更换单个组件而进行调整。每个组件具有独立的操作功能，并且通常如图2所示建造。组件110为与图1的过程步骤A对应的自热重整组件。组件120为与图1的过程步骤B对应的冷却步骤。在该描述性实施方案中，换热器121是作为组件120的常用受热器给出的。组件130为与图1的过程步骤C对应的纯化组件。组件140为与图1的过程步骤D对应的任选混合步骤。进料喷嘴131为组件140提供任选的水物流进料，以帮助推进组件150中的水气变换反应(通式IV)。组件150为与图1的过程步骤E对应的水气变换组件。进料喷嘴151为组件170中的氧化反应(通式V)的过程气体提供氧源。组件150还含有设置在催化剂床层内部或环绕催化剂床层的换热器(未画出)，从而保持所希望的水气变换反应温度。组件160为与图1的过程步骤F对应的冷却步骤。在该描述性实施方案中，换热器161是作为组件160的常用受热器给出的。组件170为与图1的过程步骤G对应的氧化步骤。组件170还含有设置在催化剂床层内部或环绕催化剂床层的换热器(未画出)，从而保持所希望的氧化反应温度。本领域的熟练技术人员应该意识到在该描述性实施方案中所描述的过程构造可以依据许多因素变化，这些因素包括原料质量和所要求的产品质量，但不局限于此。
本发明具体涉及为开车而加热催化剂床层以及在过渡操作过程中为保持所希望的反应温度而为催化剂供热的装置和方法。过渡操作包括燃料处理器的烃燃料原料变化、过程的波动、催化活性的变化、以及燃料处理器进料体积通量的升高或降低等，但不局限于此。在燃料处理器中如上面所描述的，有几种催化剂可以用于本发明，包括自热重整催化剂、部分氧化催化剂、蒸汽重整催化剂、水气变换催化剂、优先氧化催化剂以及硫吸收剂。对于燃料处理器从冷态开始有效开车来说，在这些放热性催化剂床层中将催化剂加热到反应温度是很重要的。因为紧凑型燃料处理器一种可预见的用途是用于机动车中，因此应用电加热元件的解决方案是希望的。另外，过渡操作对于确保燃料电池有稳定的富氢气体供应来说是非常重要的，其中所述富氢气体直接由燃料处理器加入。
总体来说，电加热元件可以直接或间接加热催化剂。直接加热催化剂通过使加热器元件与催化剂直接接触来实现。间接加热通过直接加热流体如工艺物流，而所述工艺物流反过来流过催化剂从而将热量传递给催化剂来实现。另外，间接加热可以通过将加热元件放置在套内，而所述套随后与催化剂或流过催化剂的流体直接接触来实现。通过这些方式，多种形式的催化剂都可以应用这种催化剂加热器，包括丸、挤出物、球以及整料。本发明的催化剂加热器可以由任何电阻丝、释热元件或棒材制成，所述加热器可以如下文所述形成。能源如电源提供能量进而产生热量。
现在参照图3，可以应用表面加热器300对催化剂床层表面310供热。在该描述性实施方案中催化剂床层表面表示圆筒状催化剂床层的一端。本领域的熟练技术人员将会意识到本发明中的催化剂床层取向可以为垂直的或水平的。在该描述性实施方案中，表面加热器300是一个沿催化剂床层表面按盘管设计形成的电加热元件，尽管可以应用其它描述性实施方案提供足够的热量传递给催化剂床层表面。通过使少量反应物流过电加热元件和催化剂床层，在催化剂床层表面引发放热反应。由表面加热器提供的热量通过催化剂床层的体积扩散，并且在催化剂床层表面产生的更多的反应热在整个催化剂床层内传播，从而为开车加热催化剂床层。该描述性实施方案的一个优选方面在于在催化剂床层的上游表面(即可以看到反应器进料的催化剂床层表面)应用表面加热器300，从而将反应热载带给“冷”的催化剂，从而提高催化剂的开车效率。
现在参照图4，电加热元件400迂回穿过(woven through)催化剂床层410。在该描述性实施方案中，电加热元件迂回穿过为丸、挤出物、球等形状的催化剂床层，或者迂回穿过整料催化剂结构。为了催化剂床层的最优加热，可以设计为迂回的设计(例如盘管)。这种描述性实施方案从催化剂内部向外供热。在加热过程中使液体流过催化剂是任选的。
现在参照图5，电加热元件500缠绕在整料催化剂结构510上。这将从催化剂外部向中心供热。在加热过程中流体流过催化剂是任选的。
另一个描述性实施方案包括在燃料处理器中的反应器，其中所述反应器包括催化剂床层、设置在催化剂床层内用于脱除正常操作中过量热量的冷却盘管，以及设置在冷却盘管内的用于在开车及过渡操作过程中将催化剂加热到所希望的反应温度的电加热元件。这是上面描述的套状加热的一个实施例。本领域的熟练技术人员应该意识到这种描述性实施方案的多种优点在于：它为催化剂快速和有效地开车供热，其预热燃料处理器的烃燃料进料，且在紧凑型燃料处理器设计中所述原料可以通过冷却盘管，并且它有助于反应器在过渡操作过程中保持反应温度。
尽管已经从优选或描述性实施方案的角度对本发明的装置、组成和方法进行了描述，但对本领域的熟练技术人员来说很明显的是在不偏离本发明的概念和范围的情况下可以对这里所描述的方法作各种改变。所有这些对本领域熟练技术人员来说很明显的类似替换和改进均应认为在本发明的范围和概念内，正如在下文权利要求中所述。

Claims (24)

1.一种为开车而加热催化剂床层的方法，包括：
提供具有上游表面和下游表面的催化剂床层；
提供沿催化剂床层一个表面设置的电加热元件；
使少量反应物通过电加热元件和催化剂床层；以及
加热电加热元件，从而在催化剂床层表面引发放热反应，其中反应热在整个催化剂床层内传播，从而为开车加热催化剂床层。
2.权利要求1的方法，其中电加热元件沿催化剂床层的上游表面设置。
3.权利要求1的方法，其中电加热元件是按盘管设计沿催化剂床层一个表面形成的。
4.权利要求1的方法，其中催化剂床层选自丸、挤出物、球、整料及其任意组合。
5.权利要求1的方法，其中催化剂床层含有选自自热重整催化剂、部分氧化催化剂、蒸汽重整催化剂、水气变换催化剂、优先氧化催化剂、阳极尾气氧化催化剂和硫吸收剂的催化剂。
6.一种用于紧凑型燃料处理器的反应器组件，包括：
具有上游表面和下游表面的催化剂床层，以及沿催化剂床层上游表面设置的电加热元件，所述加热元件能够在少量反应物存在时在催化剂床层上游表面引发放热反应。
7.权利要求6的反应器组件，其中电加热元件按盘管设计形成。
8.权利要求6的反应器组件，其中催化剂床层选自丸、挤出物、球、整料及其任意组合。
9.权利要求6的反应器组件，其中催化剂床层含有选自自热重整催化剂、部分氧化催化剂、蒸汽重整催化剂、水气变换催化剂、优先氧化催化剂、阳极尾气氧化催化剂和硫吸收剂的催化剂。
10.一种用于紧凑型燃料处理器的反应器组件，包括：
催化剂床层；
基本设置在催化剂床层内部用于在正常操作中脱除过量热量的冷却盘管；以及
设置在冷却盘管内部的电加热元件，所述加热元件能够将催化剂加热到所希望的反应温度。
11.权利要求10的反应器组件，其中催化剂床层选自丸、挤出物、球、整料及其任意组合。
12.权利要求10的反应器组件，其中催化剂床层含有选自自热重整催化剂、部分氧化催化剂、蒸汽重整催化剂、水气变换催化剂、优先氧化催化剂、阳极尾气氧化催化剂和硫吸收剂的催化剂。
13.一种加热催化剂床层的方法，包括：
提供设置在冷却盘管内部的电加热元件，所述冷却盘管基本位于催化剂床层内部；以及
加热电加热元件从而将催化剂床层加热到所希望的温度。
14.权利要求13的方法，其中所希望的温度为开车温度。
15.权利要求13的方法，其中所希望的温度为过渡操作过程中所希望的反应温度。
16.一种用于将催化剂床层加热到所希望温度的方法，包括：
提供与电加热元件相连的催化剂床层；以及
加热电加热元件，从而保持所希望的催化剂床层温度。
17.权利要求16的方法，其中所希望的温度为开车温度。
18.权利要求16的方法，其中所希望的温度为过渡操作过程中所希望的反应温度。
19.权利要求16的方法，其中电加热元件迂回穿过催化剂床层。
20.权利要求16的方法，其中催化剂床层是整料。
21.权利要求18的方法，其中电加热元件缠绕在整料上。
22.一种将催化剂床层加热到所希望温度的方法，包括：
在催化剂床层上游设置电加热元件；以及
使流体通过电加热元件并通过催化剂床层，其中将催化剂床层加热到所希望的温度。
23.权利要求22的方法，其中所希望的温度为开车温度。
24.权利要求23的方法，其中所希望的温度为过渡操作过程中所希望的反应温度。
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CA2436884A1 (en) 2002-06-13
DE60141163D1 (de) 2010-03-11
EP1347826A4 (en) 2006-05-03
AU2603902A (en) 2002-06-18
EP1345679A4 (en) 2006-05-03
CA2436868C (en) 2011-02-15
US20020090326A1 (en) 2002-07-11
NO329361B1 (no) 2010-10-04
AU2002227291B2 (en) 2007-08-30
JP2004515432A (ja) 2004-05-27
KR100798134B1 (ko) 2008-01-28
CA2436884C (en) 2010-06-22
KR20040010569A (ko) 2004-01-31
US20020090334A1 (en) 2002-07-11
WO2002047186A2 (en) 2002-06-13
WO2002045836A1 (en) 2002-06-13
BR0115948A (pt) 2004-02-25
DK1347826T3 (da) 2010-05-17
US7135154B2 (en) 2006-11-14
AU2002236584B2 (en) 2007-03-15
NO20032521D0 (no) 2003-06-04
US20070186475A1 (en) 2007-08-16
NO332183B1 (no) 2012-07-23
US7226490B2 (en) 2007-06-05
US7544346B2 (en) 2009-06-09
WO2002045838A1 (en) 2002-06-13
BR0115947A (pt) 2003-11-04
CA2436997C (en) 2010-07-20
BR0115948B1 (pt) 2010-05-18
NO20032521L (no) 2003-07-24
US20020094310A1 (en) 2002-07-18

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