201119736 六、發明說明： 【發明所屬之技術領域】 本發明係關於一種操作一或多個化學反應器的方法， 其可提高每一個反應器的操作壽命，以及關於一種反應器 ’其裝置了藉由該種方法來提高反應器操作壽命之工具。 【先前技術】 反應器的操作壽命係受到其操作條件下所承受應力的 影響。反應器能承受的應力係決定於反應器的操作溫度。 視反應器內所發生的反應而定，在整個反應器中的熱應力 可能並不均勻。即使反應器的一部分仍處於可以持續操作 相當長一段時間的狀態下，當反應器的任何一部分需要做 更換時，就需要儘快換掉反應器。 某些化學反應器係在遠距離位置運轉。例如，用來處 理伴生天然氣的反應器可能會在抽出伴生天然氣的油井附 近操作。在這些位置所用的反應器可包括，但非偈限於， 合成氣產生反應器，其係藉由蒸汽甲烷重組、自熱重組或 部分氧化反應，或者是藉由使用離子轉移薄膜來產生合成 氣；以及由合成氣來產生合成原油的Fischer-Tropsch合成 反應器。當處理伴生天然氣時，重要的是在它被產生時要 好好處理，並且當氣體無法處理時也要使反應器停機時間 最小化。如果氣體無法處理，則可能將其廢氣燃燒，而廢 氣燃燒的處罰也愈來愈嚴格。 過去曾建議過可將先前所槪述的反應用觸媒塗布在反 應器壁之上。在此情況下，觸媒壽命可能會限制了反應器 201119736 的壽命。最近則是有硏究建議可將觸媒置於反應通道內可 移除的嵌入物上，例如箔片。結果使得觸媒壽命不會再限 制反應器壽命。但取而代之的是，在反應器壽命期間，需 要週期性的停機以置換觸媒。 許多化學反應方法，包括前面所述的合成氣產生及 Fischer-Tropsch合成反應，皆需要將熱量傳遞至化學反應 物或者是由化學反應物傳遞出熱量。已提出化學反應器設 計是界定出許多第一通道，用於化學反應方法，以及許多 第二通道，用於提供或移除熱量。由於這些通道靠在一起 ，並且只有藉由一個中間器壁隔開，使得這樣的設計能夠 提供第一和第二通道之間良好的熱傳效果。舉例而言，這 種反應器可以由一疊板片所形成，其係將第一和第二流動 通道交替配置堆疊，而將此堆疊結合在一起。在那些發生 化學反應的通道中，觸媒可以安排在流動通道的壁上或者 是在***流動通道內的嵌入物上。然而，在此反應器內， 第一通道和第二通道之間會有溫度差，並且，在沿著任何 一個通道的長度方向上，事實上幾乎總是有相當明顯的溫 度差異，使得由熱膨脹所造成的機械應力是不均勻的。這 些因熱產生的應力可以降低反應器的操作壽命，其係由反 應材料的溫度而定。 在一些反應器系統中會配置集管箱，以使得流動於反 應器第一和第二通道中的流體供應至每一個反應器中。來 自反應器的輸入和輸出流係藉由導管連接，其係將來自第 一階段反應器的輸出與第二階段反應器的輸入予以連接。 201119736 爲了控制流動，也可以安裝閥。集管箱、閥和導管的配置 情形可使得每一個反應器在系統中擁有獨特的位置。在一 些反應器系統中，反應器係固定在壓力容器內，並且在此 情況下，壓力容器本身可以代替其中的一個集管箱。本發 明可同等適用於這種型態和其它型態的反應器。 【發明內容】 提出本發明係爲了滿足和減輕前面所述的部分或全部 問題。 根據本發明，其提供了一種操作一或多個化學反應器 的方法，其中每一個化學反應器界定出化學反應方法用的 第一流動通道，其係與熱傳用的第二流動通道相鄰，並且 每一個反應器皆裝有能使各個流體能在第一流動通道和第 二流動通道流動的流體連接件，其中此方法包括更改流體 經過第一流動通道或是第二流動通道或者是兩者的流動， 而改變該反應器或每一個反應器內的溫度分佈，同時在反 應器中所發生的化學反應方法仍實質上維持相同。 此方法較佳係包括以下步驟：關閉通過第一流動通道 和第二流動通道中至少一個通道之流體的流動，並且接著 改變流體連接件，並且接著重新打開流體連接件。 藉由改變反應器連續應用之間的流體連接件，可改變 每一個通道內的溫度分佈，因而改變了反應器內的熱應力 及材料溫度分佈。因而改變了反應器中熱應力最高的區域 ，結果能夠提高反應器的操作壽命。要改變流體連接件有 數種不同的方式。 201119736 流體連接件的修改較佳是在包括化學反應器之工廠維 修或停機的期間進行，或者是在化學反應器維修或停機的 期間進行。在第一個實施例中，先切斷反應器與入口和出 口管路或導管的連接，接著將反應器轉向，然後再重新連 接這些管路，使得通過反應器的流動方向反轉。或者是， 在切斷反應器之後，改變構成流體連接件的管路或導管， 並且接著重新予以連接，使得在第一流動通道或第二流動 通道或者是兩者中流動穿越反應器之流體流動方向反轉。 其中兩個反應器係串聯使用以進行兩階段反應，所以可以 交換第一和第二階段反應器。在某些情況下，可以交換第 一和第二通道的流體流動，使得在化學反應操作的下一個 階段發生在第二流動通道中。 値得一提的是’第二流動通道-也就是熱傳用的流動 通道一可以含有熱交換流體；或者是它們可以含有一種進 行第.二化學反應的流體混合物。例如，如果在第一流動通 道中的化學反應方法爲吸熱反應，其所需的熱量可以藉由 第二流動通道中的熱流體（如排氣）來供應，或者是藉由在 第二流動通道中進行放熱反應（如燃燒）來供應。另一方面 ，如果在第一流動通道中的化學反應方法爲放熱反應，需 要自第一流動通道移除的熱量可以藉由在第二流動通道中 提供冷卻劑流體來達成，或者是在第二流動通道中進行吸 熱反應來達成。 在包含數個進行相同化學反應之化學反應器的工廠中 ，反應器可以全部爲並聯或者是全部爲串聯，或者是可以 安排 ，則 本發 ，但 應了 的化 吸熱 一流 的第 動通 道內 媒嵌 進行 所存 是使 ，在 動通 仍持 二反 流動 出成 201119736 成串聯反應器的並聯組合。若化學反應器爲並聯: 當一或多個化學反應器停機時，工廠仍能持續運 明特別適用於以下情況··有一或多個化學反應器 在此同時’工廠其餘的反應器仍持續運轉。然而 解本發明亦可應用於單一反應器系統。 本發明亦提供了包含一或多個化學反應器和組合 學工廠，以用來實現該操作方法。 如果包含第一和第二流動通道之反應器中分別發 和放熱反應’且改變流體的流動係涉及交換第一 動通道中的流動時，則反應器可具有實質上相同 —流動通道和第二流動通道。這可確保裝載於第 道內的觸媒嵌入物可以同樣良好的容納於第二流 ，所以此方法也可能涉及第一和第二流動通道之 入物的交換（然而，如果通道內的觸媒相同，就不 交換）。通道具有相同尺寸可同時確保在每一個構 在的反應體積及熱傳條件是相同的，所以反應器 用何種構形皆會在實質上具有相同的表現方式。 這樣的情況下，在流動改變之前和之後，於每一 道中進行的是不同的化學反應，雖然反應器整體 續進行相同的化學反應方法。 此外’依據本發明其提供了一種包含第一反應器 應器的模組，每一個反應器具有第一流動通道和 通道’以及導管（其裝配的目的係將第一反應器 爲第二反應器的輸入），以及旁通導管和閥（其裝 作 轉。 停機 ，亦 裝置 生了 和第 大小 —流 動通 間觸 需要 形中 姐論 ytv? 口 問 因此 組流 而言 和第 第二 的輸 配的 201119736 目的係將第二反應器的輸出成爲第一反應器的輸入）。提供 能使流動反轉之模組（包含兩個反應器以及導管和閥）可以 讓爲了達到通過第一反應器和第二反應器內之流動方向反 轉所需在現址進行的工作降至最低。因此，在這種情況下 ，操作的效果係改變反應器進行兩階段方法中的那一個階 段；但是模組所進行的化學反應方法並沒有改變。 本發明可適用於任何具有多重反應通道的反應器。反 應器本身可以包括一疊板片。舉例而言，可以在各個板片 中藉由溝槽來界定第一和第二流動通道，將板片予以堆疊 ，然後接合在一起。或者是，可藉由成波浪狀或城堡狀且 與扁平薄片交替堆疊的薄金屬片來界定流動通道；流動通 道的邊緣可以用密封條定出界限。又或者是，可藉由間隔 條將扁平薄片隔開的方式來界定流動通道。爲能確保達到 所需的良好熱接觸，第一和第二流動通道可以介於10毫米 到0.5毫米高之間（在流動方向上）；並且每一個通道的寬度 可以介於約1毫米到5 0毫米之間。形成一組反應器的板片 堆疊可以藉由（例如）擴散接合、硬銲或熱等力加壓等方式 接合在一起。第一和第二流動通道的本質須由反應器中所 發生的反應來決定。例如，放熱化學反應用通道可在堆叠 中與吸熱反應用通道交替配置；在此情況下，在每一個通 道中必須放置適當的觸媒。例如，放熱反應可以是燃燒反 應’並且吸熱反應可以是蒸汽甲烷重組。在其它例子中， 化學反應用通道（第一通道）可在堆疊中與熱傳介質（如冷卻 劑）用通道交替配置。舉例而言，第一通道可以是用來進行 201119736201119736 VI. Description of the Invention: [Technical Field] The present invention relates to a method of operating one or more chemical reactors, which can improve the operational life of each reactor, and A tool for increasing the operational life of the reactor by this method. [Prior Art] The operational life of the reactor is affected by the stresses experienced under its operating conditions. The stress that the reactor can withstand is determined by the operating temperature of the reactor. Depending on the reaction occurring within the reactor, the thermal stress throughout the reactor may not be uniform. Even if a part of the reactor is still in a state where it can be operated for a long period of time, when any part of the reactor needs to be replaced, it is necessary to replace the reactor as soon as possible. Some chemical reactors operate at remote locations. For example, a reactor used to treat associated natural gas may operate near a well that draws associated natural gas. The reactors used at these locations may include, but are not limited to, a syngas generating reactor which is produced by steam methane recombination, autothermal recombination or partial oxidation, or by using an ion transport membrane to produce syngas; And a Fischer-Tropsch synthesis reactor from syngas to produce synthetic crude oil. When dealing with associated natural gas, it is important to handle it as it is produced and to minimize reactor downtime when the gas cannot be processed. If the gas cannot be disposed of, the exhaust gas may be burned, and the penalty for burning the exhaust gas is becoming more stringent. It has been suggested in the past that the previously described reaction catalyst can be applied over the reactor wall. In this case, catalyst life may limit the life of the reactor 201119736. Recently, it has been suggested that the catalyst can be placed on a removable insert in the reaction channel, such as a foil. As a result, catalyst life does not limit reactor life. Instead, cyclical shutdowns are required to displace the catalyst during the life of the reactor. Many chemical reaction processes, including the syngas generation and Fischer-Tropsch synthesis reactions described above, require heat transfer to the chemical reactants or transfer of heat from the chemical reactants. It has been proposed that the chemical reactor design defines a number of first channels for chemical reaction methods, as well as a number of second channels for providing or removing heat. Since these channels are close together and separated by only one intermediate wall, such a design provides a good heat transfer between the first and second channels. For example, such a reactor can be formed from a stack of sheets that alternately stack the first and second flow channels and bond the stack together. In those channels where the chemical reaction takes place, the catalyst can be arranged on the wall of the flow channel or on the insert inserted into the flow channel. However, in this reactor, there is a temperature difference between the first passage and the second passage, and in the length direction along any one of the passages, there is almost always a fairly significant temperature difference, so that the thermal expansion The resulting mechanical stress is not uniform. These stresses due to heat can reduce the operational life of the reactor, depending on the temperature of the reaction material. A header tank is configured in some reactor systems to supply fluid flowing in the first and second passages of the reactor to each of the reactors. The input and output streams from the reactor are connected by a conduit that connects the output from the first stage reactor to the input of the second stage reactor. 201119736 Valves can also be installed to control flow. The configuration of headers, valves, and conduits allows each reactor to have a unique location in the system. In some reactor systems, the reactor is fixed in a pressure vessel, and in this case, the pressure vessel itself can replace one of the headers. The invention is equally applicable to reactors of this type and other types. SUMMARY OF THE INVENTION The present invention has been made to satisfy and alleviate some or all of the problems described above. According to the present invention, there is provided a method of operating one or more chemical reactors, wherein each chemical reactor defines a first flow channel for a chemical reaction process adjacent to a second flow channel for heat transfer And each of the reactors is provided with a fluid connection that enables each fluid to flow in the first flow channel and the second flow channel, wherein the method includes modifying the fluid through the first flow channel or the second flow channel or two The flow of the person changes the temperature distribution within the reactor or each reactor while the chemical reaction process occurring in the reactor remains substantially the same. Preferably, the method includes the steps of closing the flow of fluid through at least one of the first flow passage and the second flow passage, and then changing the fluid connection, and then reopening the fluid connection. By varying the fluid connections between successive applications of the reactor, the temperature profile within each channel can be varied, thereby altering the thermal stress and material temperature distribution within the reactor. Thus, the region with the highest thermal stress in the reactor is changed, and as a result, the operational life of the reactor can be improved. There are several different ways to change the fluid connection. 201119736 The modification of the fluid connection is preferably carried out during maintenance or shutdown of the plant including the chemical reactor, or during the maintenance or shutdown of the chemical reactor. In the first embodiment, the connection of the reactor to the inlet and outlet lines or conduits is first shut off, then the reactor is turned and then reconnected to reverse the flow direction through the reactor. Alternatively, after the reactor is shut off, the tubing or conduit forming the fluid connection is changed and then reconnected such that fluid flow through the reactor in either the first flow channel or the second flow channel or both The direction is reversed. Two of the reactors are used in series for the two-stage reaction, so the first and second stage reactors can be exchanged. In some cases, the fluid flow of the first and second passages may be exchanged such that the second flow passage occurs in the next stage of the chemical reaction operation. It is noted that the 'second flow channels' - that is, the flow channels for heat transfer - may contain heat exchange fluids; or they may contain a fluid mixture for the second chemical reaction. For example, if the chemical reaction method in the first flow channel is an endothermic reaction, the heat required may be supplied by a hot fluid (such as exhaust gas) in the second flow channel, or by the second flow channel. An exothermic reaction (such as combustion) is carried out to supply. On the other hand, if the chemical reaction method in the first flow channel is an exothermic reaction, the heat required to be removed from the first flow channel can be achieved by providing a coolant fluid in the second flow channel, or in the second An endothermic reaction is carried out in the flow channel to achieve. In a plant containing several chemical reactors that perform the same chemical reaction, the reactors may all be in parallel or all in series, or may be arranged, but the present invention, but the first end of the first-pass channel The in-line operation is such that the U-turn still holds the two-reverse flow into a parallel combination of the 201119736 series reactor. If the chemical reactors are in parallel: When one or more chemical reactors are shut down, the plant can continue to operate particularly well in the following situations: • One or more chemical reactors at the same time 'The rest of the plant's reactors continue to operate . However, the invention can also be applied to a single reactor system. The invention also provides for the inclusion of one or more chemical reactors and combinatorial plants for carrying out the method of operation. If separate and exothermic reactions are present in the reactor containing the first and second flow channels and changing the flow of the fluid involves exchanging the flow in the first moving channel, then the reactors can be substantially identical - the flow channels and the second Flow channel. This ensures that the catalyst insert loaded in the first lane can be equally well accommodated in the second stream, so this method may also involve the exchange of the first and second flow channels (however, if the catalyst is in the channel) The same, they are not exchanged). The channels are of the same size to ensure that the reaction volume and heat transfer conditions are the same at each configuration, so that the configuration of the reactor will have essentially the same behavior. In such a case, different chemical reactions are carried out in each lane before and after the flow change, although the reactor continues to undergo the same chemical reaction method as a whole. Furthermore, according to the invention there is provided a module comprising a first reactor, each reactor having a first flow channel and a channel' and a conduit (the purpose of which is to assemble the first reactor to be a second reactor) The input), as well as the bypass conduit and valve (which is installed as a turn. The shutdown, the device is also born and the size - the flow through the touch needs to be in the form of a ytv? Interrogation so the flow and the second loss The purpose of 201119736 is to make the output of the second reactor the input to the first reactor). Providing a module capable of reversing the flow (containing two reactors and conduits and valves) allows the work at the current site to be reduced in order to achieve a reversal of the flow direction through the first reactor and the second reactor lowest. Therefore, in this case, the effect of the operation is to change the stage in which the reactor performs the two-stage method; however, the chemical reaction method performed by the module does not change. The invention is applicable to any reactor having multiple reaction channels. The reactor itself can include a stack of sheets. For example, the first and second flow channels can be defined by grooves in each of the sheets, the sheets are stacked, and then joined together. Alternatively, the flow passage may be defined by a thin metal sheet which is wavy or castle-like and alternately stacked with the flat sheets; the edges of the flow passages may be defined by the seal strips. Still alternatively, the flow channels can be defined by spacing the flat sheets apart by spacers. In order to ensure that the desired good thermal contact is achieved, the first and second flow channels may be between 10 mm and 0.5 mm high (in the flow direction); and each channel may have a width of between about 1 mm and 5 Between 0 mm. The stack of sheets forming a set of reactors can be joined together by, for example, diffusion bonding, brazing or heat or the like. The nature of the first and second flow channels must be determined by the reactions occurring in the reactor. For example, the channels for exothermic chemical reactions can be alternately arranged in the stack with the channels for endothermic reactions; in this case, appropriate catalyst must be placed in each channel. For example, the exothermic reaction can be a combustion reaction' and the endothermic reaction can be a steam methane recombination. In other examples, the chemical reaction channels (first channels) may be alternately arranged with the heat transfer medium (e.g., coolant) in the stack. For example, the first channel can be used to carry out 201119736
Fischer-Tropsch反應，並且在此例子中的熱傳介質爲冷卻 劑。如果觸媒係置於可移除的嵌入物之上，含觸媒之通道 較佳係具有至少2毫米的高度及至少2毫米的寬度。本發 明可適用於其它反寧器型態，並且在替代的反應器方面， 可以包含殼和管。 當以可移除嵌入物做爲觸媒載體時，其可包括一或多 個波浪狀的箔片。觸媒也可置於網目、泡沬或毛氈上。在 每一個例子，觸媒載體可以形成部分反應器結構，或是非 結構的。或者是，可將觸媒置放於通道內部表面之上。在 某些例子中，觸媒可以爲九狀。 【實施方式】 現在將藉由實施例並且參考附圖，針對本發明做進一 步及更特別的描述： 第1圖顯示的是兩階段蒸汽甲烷重組反應器模組的示 意圖。 第2圖顯示的是第1圖之反應器模組內的溫度變化情 形。 首先參考第1圖，其顯示的是適合用來做爲蒸汽重組 反應器的反應模組1 〇。反應器模組1 0係由兩個反應器區 塊12a和12b所構成，每一個區塊則是由一疊平面俯視爲 矩形的板片所構成，每一個平板皆爲耐腐蝕高溫的合金。 扁平板片係與城堡狀板片交替配置以界定出區塊1 2a或 12b兩端之間的流動通道，每一個通道的長度爲600毫米 ，在其間可發生反應。所有的通道彼此平行延伸’有集管 -10 - 201119736 箱可以將蒸汽/甲烷混合物提供至第15 ’ Μ·0*% 空氣/甲烷混合物提供至第二組通道16 ’第—和1第— 在此堆疊中交替（通道1 5和1 6係槪略性地示意代表）’使 得堆疊頂端和底部的通道皆爲燃燒通道16°用&名應' 的適當觸媒可以置於通道15和16中的波浪狀箱片（圖中未 顯示）上。在每一個燃燒通道16的入口處裝設滅焰器17° 反應器區塊12a和12b所示爲槪略圖’特別是在每—端安 排的集管箱並未於圖中顯示。 蒸汽/甲烷混合物被安排流過串聯的反應器區塊12a 和12b，有導管20將第一反應器區塊l2a之通道15的出 口到第二反應器區塊12b之通道15的入口將以連接。同樣 的，燃燒混合物也是流過串聯的反應器區塊12&和12b’ 有導管22將第一反應器區塊12a之通道16的出口到第二 反應器區塊12b之通道16的入口將以連接。導管22包括 額外空氣用的入口 24，接著爲靜態攪拌機25’然後是額外 燃料用的入口 26，接著爲另一個靜態攪拌機27。 在使用反應模組1〇時，蒸汽/甲烷混合物被預熱並且 供應至反應模組1〇。將80%所需空氣和60%所需甲烷（做爲 燃料）所形成之混合物予以預熱’並且供應至第一反應器區 塊12a。在觸媒處燃燒的結果造成了溫度上升。向外流動 的熱氣體與剩餘20%的所需空氣混合（藉由入口 24和靜態 攪拌機25來進行），接著再與剩餘40%的所需甲烷混合（藉 由入口 26和靜態攪拌機27來進行），並且供應至第二反應 器區塊12b的燃燒通道16。 201119736 現在再參考第2圖，其係顯示溫度T沿著燃燒通道1 6 ( 標示爲Α)之長度L以及沿著重組通道15(標示爲Β)的變化 圖形。圖中介於L = 0和L = 0.6公尺之間的部分係相當於第 一反應器區塊12a，而圖中介於L = 0.6公尺和L=1.2公尺之 間的部分則是相當於第二反應器區塊1 2b °値得注意的是 :一旦開始進行燃燒，重組通道1 5中的溫度T永遠會低於 相鄰燃燒通道16中的溫度T。燃燒氣體溫度會因爲第一反 應器區塊12a和第二反應器區塊12b之間（在L = 0.6公尺的 位置）所添加的空氣（來自入口 24)而進行向下的階段性改 變。 藉由調整燃燒通道和重組通道中的空間速度’以及調 整用於燃燒而提供至每一個反應器區塊之燃料及空氣的比 例，可以調整反應器區塊12a和12b內的溫度分佈。溫度 的變動，尤其是第一和第二流動通道之間的溫度差異，以 及沿著通道長度方向上的溫度變動，係反應器區塊結構中 發生熱應力的原因；雖然可以藉由改變溫度分佈的方式來 降低熱應力，它們無法被消除。在這個實施例中，也應認 知到，在第一階段反應器區塊12a中的溫度變動會大於第 二階段反應器區塊12b的變動。 反應模組10可形成化學工廠的一部分，由反應模組 10所產生的合成氣被接著進料至工廠的其它反應器中，以 產生其它產物。工廠可合倂數個並聯安排的反應模組1 0 , 使得合成氣的生產可以藉由改變使用反應模組10的數字 而加以調整。在這個情況下，可以關閉一個模組，例如進 -12- 201119736 行維修，但是不用關閉工廠的其它部分。在任何情況下， 無論是只有一個此類的反應模組10或者是數個反應模組 1 〇，偶爾總是需要關閉反應模組1 0以進行維修或服務，例 如置換失效的觸媒。當反應模組10被關閉時，就提供了一 個依照本發明來進行改變的機會。 例如，反應器區塊12a，可以切斷它的入口和出口導 管，並且反應器區塊12a可以接著被轉向，並且接著重新 連接導管，使得通過反應器區塊12a的流動方向反轉。或 者是，它可以更方便的讓反應器區塊12a留在原位置，並 且在切斷反應器區塊12a之後，可將其所伴隨的入口和出 口導管延伸並且連接，使得通過反應器區塊12a的流動方 向反轉。在這個實施例中，較佳是使與第一流動通道15和 第二流動通道16連通的導管皆接受這些改變，以確保流動 能夠持續爲順流。在其它反應器中，較佳是讓這樣的改變 只發生在這些通道組合的其中一組。應了解，這樣的改變 可以同樣發生在其它反應器區塊12b，可以是替代反應器 區塊12a發生改變，或者是兩者同時發生改變。當通過燃 燒通道16的流動方向反轉時，可將滅焰器17由通道16的 —端移到另一端，或者是將滅焰器17同時置放於通道16 的兩端。 本發明不只是適用於藉由在熱傳通道內的催化燃燒來 提供熱量之反應器，同時亦適用於藉由外部燃燒反應產生 熱氣體並使熱氣體流入熱傳通道來提供熱量之反應器。 還有另一個替代選擇，如果用於第一反應（蒸汽甲烷重 -13- 201119736 組）的觸媒也適合用於第二反應（燃燒）且反之亦然時，則可 以切斷導管與反應器區塊（也就是反應器區塊12a)的連 接，並且接著與其它組通道重新連接。在這個實施例中， 必需將蒸汽/甲烷混合物供應至第二組通道16，並且將空 氣/甲烷混合物供應至第一組通道15»如果觸媒不能同時 適用於兩種反應，則可將觸媒自通道15和自通道16中移 除，並且嵌入其它組通道內。這通常會涉及部分或完全失 效觸媒的移除和嵌入新鮮觸媒。在這個實施例中，通道15 和通道16較佳是具有相同的尺寸，使得相同的觸媒可置入 通道中，並且在改變之後所提供的反應體積也與改變之前 相同。同樣應了解的是，其它反應器區塊12b可以做這樣 的改變，可以是替代反應器區塊12a發生改變，或者是兩 者同時發生改變。 在這個實施例中，做爲另一種替代選項，可以同時切 斷反應器12a和12b，並且交換位置，接著再重新連接， 使得反應的第一階段發生在反應器區塊12b，且第二階段 發生在反應器區塊12a。這可能涉及移動反應器區塊本身 ，或者是讓反應器區斑留在原位並且改變流動導管。 應了解工廠可包括適合用來產生流動方向反轉的導管 ，因此，它只需要改變閥的位置。這可由第1圖中所示甲 烷和蒸汽進入第一階段反應器區塊12a的流動而得到了解 。爲此目的，可在導入第一流動通道15入口的導管中配置 關斷閥30，並且可在由第一流動通道15出口導出的導管 中配置關斷閥32。入口旁通導管34 (以虛線標示）係連通關 -14- 201119736 斷閥30上游和關斷閥32上游之間’且出口旁通導管36( 以虛線標示）係連通關斷閥3 0下游和關斷閥3 2下游之間。 入口旁通導管34和出口旁通導管36皆在兩端裝設了關斷 閥3 5。在操作之初，關斷閥3 0和3 2皆是打開的，然而所 有的關斷閥3 5則是關閉的。因此，如先前所述’甲烷和蒸 汽.混合物係沿著流動通道1 5自左邊流向右邊穿過反應區 塊12a。當流動方向反轉時，關斷閥30和32皆被關閉’ 然而所有的關斷閥35則是打開的。在這個情況下，甲烷和 蒸汽混合物沿著入口旁通導管34流動，接著沿著流動通道 由右至左流動，然後再沿著出口旁通導管36流動。應了解 的是：對於提供至第一階段反應器區段12a的燃燒氣體也 可以提供類似的入口和出口旁通導管及關斷閥的配置方式 。也應瞭解到第二階段反應器區塊12b可以用相同的方式 修改成此類旁通導管和關斷閥。 在反應器區塊（也就是區塊12a)做了改變之後，當模組 10再回復使用時，熱應力將會影響反應器區段12a的不同 部分。因此，反應器區段中承受最大熱應力的部分會由初 始的部分改變到不同的部分，所以，如果反應器區塊有任 何退化是因爲應力而造成時，初始部分的進一步退化將會 被抑制，並且後續的退化將發生在不同部分。因此，反應 器區塊的操作壽命可以被提高。 雖然本發明已針對兩階段蒸汽甲烷重組模組來加以描 述，但應了解，它可以應用於任何具有反應通道和熱傳通 道的化學反應器，無論是單階段或是多階段。舉例而言， -15- •201119736 本發明適合用於部分氧化反應器， ，其係用來製造合成氣的另一種反 進行Fischer-Tropsch合成的反應器 行的放熱反應，並且在這個例子中 但是第二流動通道只裝塡了冷卻劑 作一段時間之後，將反應器停機， 關聯之入口和出口導管的連結，並 或者是讓反應器區塊留在原來的位 管；無論是那一個例子，這些改變 器區塊的流動方向反轉。或者是， 聯反應器之反應器模組來進行Fis< 由於合成反應是在兩個階段中發生 ，將反應器模組停機，然後將形成 〇 在另一個替代方案中，特別可 作反應模組的工廠，可以改變供應 ，例如增加20% ;在此同時，將流 反應劑減少20%，使得通過工廠的 樣的變化會影響每一個模組之反應 經過一段時間之後，例如在一個星 至每一個模組之反應劑的量減少， 反應劑的量予以增加，使得每一個 度分佈再次改變。重覆進行這樣的 的有害影響。 或者是自熱重組反應器 應器。它也可以應用於 。這是一種在高壓下進 ，第一通道含有觸媒， 。在這個例子中，在操 並切斷反應器區塊與它 且將反應器區塊轉向； 置，改變入口和出口導 可確保反應劑流經反應 如果是使用含有兩個串 her-Tropsch合成反應， ，在操作一段時間之後 模組的反應器予以交換 應用於含有數個並聯操 至模組之反應劑的流動 動至另一個平行模組的 流動總量沒有改變。這 器內部的溫度分佈。在 期或一個月之後，將流 而流到其它平行模組之 模組之反應器內部的溫 改變，可以減緩熱應力 •16- 201119736 【圖式簡單說明】 第1圖顯示的是兩階段蒸汽甲烷重組反應器模組的示 意圖。 第2圖顯示的是第1圖之反應器模組內的溫度變化情 形。 【主要元件符號說明】 10 反應模組 12a 反應器區塊 12b 反應器區塊 15 通道 16 通道 17 滅焰器 20 導管 22 導管 24 入口 25 靜態攪拌機 26 入口 27 靜態攪拌機 30 關斷閥 32 關斷閥 34 旁通導管 3 5 關斷閥 36 旁通導管 -17-The Fischer-Tropsch reaction, and the heat transfer medium in this example is a coolant. If the catalyst is placed over the removable insert, the channel containing the catalyst preferably has a height of at least 2 mm and a width of at least 2 mm. The invention is applicable to other reactor types and may include shells and tubes in alternative reactors. When the removable insert is used as a catalyst carrier, it may include one or more wavy foils. The catalyst can also be placed on a mesh, foam or felt. In each of the examples, the catalyst carrier can form part of the reactor structure, or be unstructured. Alternatively, the catalyst can be placed over the interior surface of the channel. In some instances, the catalyst can be nine-shaped. [Embodiment] A further and more specific description of the present invention will now be made by way of embodiments and with reference to the accompanying drawings. FIG. 1 shows a schematic diagram of a two-stage steam methane recombination reactor module. Figure 2 shows the temperature variation in the reactor module of Figure 1. Referring first to Figure 1, there is shown a reaction module 1 适合 suitable for use as a steam reforming reactor. The reactor module 10 is composed of two reactor blocks 12a and 12b, each of which is composed of a stack of rectangular plates in plan view, each of which is a corrosion-resistant high-temperature alloy. The flat sheets are alternately arranged with the castellated sheets to define flow passages between the ends of the blocks 12a or 12b, each of which has a length of 600 mm, during which a reaction can occur. All channels extend parallel to each other 'with header-10 - 201119736 box can supply steam/methane mixture to 15 ' Μ · 0*% air/methane mixture provided to the second group of channels 16 '-- and 1st - in Alternate in this stack (channels 15 and 16 are slightly represented) 'so that the top and bottom channels of the stack are both the combustion channel 16° and the appropriate catalyst for the name should be placed in channels 15 and 16 On the wavy box (not shown). A flame arrester 17 is installed at the entrance of each of the combustion passages 16. The reactor blocks 12a and 12b are shown in a schematic view, and in particular, the headers arranged at each end are not shown. The steam/methane mixture is arranged to flow through the reactor blocks 12a and 12b in series, with a conduit 20 connecting the outlet of the passage 15 of the first reactor block 12a to the inlet 15 of the second reactor block 12b. . Similarly, the combustion mixture also flows through the reactor blocks 12& and 12b' in series with the conduit 22 connecting the outlet of the passage 16 of the first reactor block 12a to the passage 16 of the second reactor block 12b. connection. The conduit 22 includes an inlet 24 for additional air, followed by a static mixer 25' followed by an inlet 26 for additional fuel, followed by another static mixer 27. When the reaction module 1 is used, the steam/methane mixture is preheated and supplied to the reaction module 1〇. A mixture of 80% of the desired air and 60% of the desired methane (as a fuel) is preheated' and supplied to the first reactor block 12a. The result of combustion at the catalyst causes a temperature rise. The outward flowing hot gas is mixed with the remaining 20% of the desired air (by inlet 24 and static mixer 25), followed by the remaining 40% of the desired methane (by inlet 26 and static mixer 27). And supplied to the combustion passage 16 of the second reactor block 12b. 201119736 Referring now again to Figure 2, there is shown a graph of the temperature T along the length L of the combustion channel 16 (labeled Α) and along the recombination channel 15 (labeled Β). The portion between L = 0 and L = 0.6 m in the figure corresponds to the first reactor block 12a, and the portion between L = 0.6 m and L = 1.2 m in the figure is equivalent. The second reactor block 1 2b ° is noted that once combustion is initiated, the temperature T in the recombination channel 15 will always be lower than the temperature T in the adjacent combustion channel 16. The combustion gas temperature undergoes a downward phase change due to the added air (from the inlet 24) between the first reactor block 12a and the second reactor block 12b (at the L = 0.6 meter position). The temperature distribution within the reactor blocks 12a and 12b can be adjusted by adjusting the space velocity in the combustion and recombination channels and adjusting the ratio of fuel and air supplied to each of the reactor blocks for combustion. The change in temperature, especially the temperature difference between the first and second flow channels, and the temperature variation along the length of the channel, are the cause of thermal stress in the reactor block structure; although it is possible to change the temperature distribution The way to reduce thermal stress, they cannot be eliminated. In this embodiment, it will also be appreciated that the temperature variation in the first stage reactor block 12a will be greater than the variation in the second stage reactor block 12b. The reaction module 10 can form part of a chemical plant, and the syngas produced by the reaction module 10 is then fed to other reactors in the plant to produce other products. The plant can combine a plurality of reaction modules 10 arranged in parallel so that the production of syngas can be adjusted by changing the number of the reaction module 10 used. In this case, you can close a module, for example, to -12-201119736 for maintenance, but do not need to close other parts of the plant. In any case, whether there is only one such reaction module 10 or a plurality of reaction modules, it is occasionally necessary to turn off the reaction module 10 for maintenance or service, such as replacing a failed catalyst. When the reaction module 10 is turned off, an opportunity to make changes in accordance with the present invention is provided. For example, reactor block 12a, its inlet and outlet conduits can be severed, and reactor block 12a can then be diverted and the conduit then reconnected such that the flow direction through reactor block 12a is reversed. Alternatively, it may be more convenient to leave the reactor block 12a in place, and after shutting down the reactor block 12a, its associated inlet and outlet conduits may be extended and connected such that passage through the reactor block 12a The flow direction is reversed. In this embodiment, it is preferred that the conduits in communication with the first flow passage 15 and the second flow passage 16 accept these changes to ensure that the flow continues to be downstream. In other reactors, it is preferred that such changes occur only in one of these channel combinations. It will be appreciated that such changes may occur equally in other reactor blocks 12b, either in the alternative reactor block 12a, or at the same time. When the flow direction through the combustion passage 16 is reversed, the flame extinguisher 17 can be moved from the end of the passage 16 to the other end, or the flame extinguisher 17 can be simultaneously placed at both ends of the passage 16. The present invention is not only applicable to a reactor for supplying heat by catalytic combustion in a heat transfer passage, but also to a reactor for generating heat by generating a hot gas by an external combustion reaction and flowing the hot gas into the heat transfer passage. There is another alternative, if the catalyst used in the first reaction (steam methane weight -13 - 201119736 group) is also suitable for the second reaction (combustion) and vice versa, the conduit and reactor can be shut off. The block (i.e., reactor block 12a) is connected and then reconnected to the other group channels. In this embodiment, it is necessary to supply the steam/methane mixture to the second set of channels 16 and supply the air/methane mixture to the first set of channels 15» if the catalyst cannot be applied to both reactions at the same time, the catalyst can be used It is removed from channel 15 and from channel 16 and embedded in other group channels. This usually involves the removal of partially or completely catastrophic catalysts and the embedding of fresh catalysts. In this embodiment, the channel 15 and the channel 16 are preferably of the same size such that the same catalyst can be placed in the channel and the reaction volume provided after the change is also the same as before the change. It should also be understood that other reactor blocks 12b may be modified such that the replacement reactor block 12a changes, or both change at the same time. In this embodiment, as an alternative, the reactors 12a and 12b can be shut off simultaneously, and the position exchanged, followed by reconnection, such that the first stage of the reaction occurs in the reactor block 12b, and the second stage Occurs in reactor block 12a. This may involve moving the reactor block itself, or leaving the reactor zone in place and changing the flow conduit. It should be understood that the plant may include a conduit suitable for generating a reversal of the flow direction, so that it only needs to change the position of the valve. This is understood by the flow of methane and steam shown in Figure 1 into the first stage reactor block 12a. For this purpose, the shut-off valve 30 can be configured in the conduit leading to the inlet of the first flow passage 15, and the shut-off valve 32 can be disposed in the conduit leading from the outlet of the first flow passage 15. The inlet bypass conduit 34 (indicated by the dashed line) is connected between the closing -14, 19, 1973, the upstream of the shut-off valve 30 and the upstream of the shut-off valve 32, and the outlet bypass conduit 36 (indicated by the dashed line) is connected downstream of the shut-off valve 30 and Shut off the valve 3 2 between the downstream. Both the inlet bypass conduit 34 and the outlet bypass conduit 36 are provided with shut-off valves 35 at both ends. At the beginning of the operation, the shut-off valves 30 and 3 2 are all open, however all the shut-off valves 35 are closed. Thus, as previously described, the 'methane and steam. mixture flows from the left to the right along the flow channel 15 through the reaction block 12a. When the flow direction is reversed, the shut-off valves 30 and 32 are both closed. However, all of the shut-off valves 35 are open. In this case, the methane and steam mixture flows along the inlet bypass conduit 34, then flows from right to left along the flow passage, and then flows along the outlet bypass conduit 36. It will be appreciated that similar inlet and outlet bypass conduits and shut-off valves may be provided for the combustion gases provided to the first stage reactor section 12a. It should also be understood that the second stage reactor block 12b can be modified in the same manner as such bypass conduits and shut-off valves. After the reactor block (i.e., block 12a) has been changed, thermal stress will affect different portions of the reactor section 12a when the module 10 is returned to service. Therefore, the portion of the reactor section that is subjected to the greatest thermal stress will change from the initial portion to the different portion, so if any degradation of the reactor block is due to stress, further degradation of the initial portion will be inhibited. And subsequent degradation will occur in different parts. Therefore, the operational life of the reactor block can be improved. Although the invention has been described in terms of a two-stage steam methane recombination module, it should be understood that it can be applied to any chemical reactor having a reaction channel and a heat transfer channel, either in a single stage or in multiple stages. For example, -15- • 201119736 The present invention is suitable for use in a partial oxidation reactor, which is used to produce an exothermic reaction of another reactor gas that is subjected to Fischer-Tropsch synthesis, and in this example but The second flow channel is only installed with the coolant for a period of time, the reactor is shut down, the associated inlet and outlet conduits are connected, or the reactor block is left in the original position tube; in either case, The flow direction of these modifier blocks is reversed. Alternatively, the reactor module of the reactor is used to perform Fis< because the synthesis reaction occurs in two stages, the reactor module is shut down, and then the crucible is formed in another alternative, particularly as a reaction module. The factory can change the supply, for example by 20%; at the same time, reduce the flow reactant by 20%, so that changes in the factory will affect the reaction of each module after a period of time, for example, in a star to each The amount of reactants in one module is reduced and the amount of reactants is increased such that each degree distribution changes again. Repeat such harmful effects. Or an autothermal recombination reactor. It can also be applied to. This is a kind of high pressure, and the first channel contains a catalyst. In this example, the reactor block is operated and shut off and the reactor block is turned; setting, changing the inlet and outlet conductors ensures that the reactants flow through the reaction if it is used to contain two strings of her-Tropsch synthesis reactions. After the operation for a period of time, the reactor of the module is exchanged for application to the flow of the reactants containing several parallel operations to the module, and the total flow of the flow to the other parallel module is not changed. The temperature distribution inside the device. After a period of one month or a month, the temperature change inside the reactor flowing to the modules of other parallel modules can slow down the thermal stress. 16-201119736 [Simplified Schematic] Figure 1 shows the two-stage steam Schematic diagram of a methane recombination reactor module. Figure 2 shows the temperature variation in the reactor module of Figure 1. [Main component symbol description] 10 Reaction module 12a Reactor block 12b Reactor block 15 Channel 16 Channel 17 Flame arrester 20 Catheter 22 Catheter 24 Inlet 25 Static mixer 26 Inlet 27 Static mixer 30 Shut-off valve 32 Shut-off valve 34 Bypass conduit 3 5 Shutoff valve 36 Bypass conduit-17-