201000844 六、發明說明： 【發明所屬之技術領域】 本發明係關於一種供溫度敏感性及/或可聚合之產物 用的熱交換器。 【先前技術】 相關文獻揭示了許多不同態樣的熱交換器，因此舉例 來說，由平板熱交換器或微熱交換器構成之熱交換器類型 適合短逗留時間。然而，此類熱交換器具有肇因於狹小流 量缺口的缺點，其僅適用於低黏度產物。在更高黏度產物 的例子中，遍及這些熱交換器各處的失壓可能非常高。在 產物傾向聚合的例子中，例如單體或是仍含有單體的聚合 物漿料，其具有在熱交換器操作期間或終止時單體將聚合 的危險性。將已聚合的漿料由平板熱交換器及微熱交換器 移出若非不可能的話是非常複雜的。對高黏度，特別是數 帕•秒，及高於1 〇巴的高壓而言，由於製造方法及所產生 的力之故，沒有任何平板熱交換器可供使用。 美國1,96 1，907號專利描述了一種管束熱交換器，於其 管中具有螺旋溝槽置換體。由於其螺旋狀的流動，使得以 達成特別有效的熱交換。然而，由於待調溫的介質於置換 管中流動，產生額外的失壓及額外的逗留時間，此可能對 產物造成傷害。更進一步地，複雜的設計也導致高成本、 難以拆卸及困難的淨空程序。 德國-G 87 12 8 1 5 ( VIA Gesellschaft fur Verfahrenstechnik) 201000844 描述一種壓縮空氣乾燥器的管束熱交換器，爲節省材料， 導入管中的置換體依序含有一接近注入端的管。置換管可 具有一具凹槽的表面。然而，因爲不使用非常小逗留（ hold-up )的托盤以及置換桿並不接近底部，此設計（並非 針對溫度敏感性產物而開發）因此具有大的產物塡充體積 。此外，由於置換管無法拆卸，這對溫度敏感性聚合物的 例子構成主要的缺點。 德國 DE-G 89 03 349 ( VIA Gesellschaft fiir Verfahrenstechnik )揭示了 一種管束熱交換器，特別係用於壓縮空氣乾燥器 。爲使熱轉移介質能儘可能地均勻流過裝置，於該裝置中 設置一確保均勻流向管的有孔平板。然而，在此管束熱交 換器的例子中，在溫和條件下的熱轉移是不必要的，因此 對於置換桿截面並沒有特殊的要求，且不需要具有最小逗 留的置換蓋或平板托盤。更進一步地，置換桿無法拆卸。 在相對高黏度產物的例子中呈現小失壓的熱交換器是 常見的，例如管束類型。在此實施態樣中，產物流穿數個 平行排列的管。然而，此處的缺點係管束熱交換器通常具 有一小而特殊的熱交換空間。該特殊的熱交換空間在此係 定義爲熱交換區域與管中塡充產物的體積之比例。因爲該 小的熱交換空間，通常因而需要管中具有相當大的托量之 熱交換器。該管束熱交換器的逗留時間因此非常高。 【發明內容】 鑑於前述先前技術，本發明之目的在開發一種可使待 -6- 201000844 加熱或待冷卻的產物在熱交換器中的逗留時間儘可能地短 的熱交換器。該熱交換器應進一步被設計成低黏度或更高 黏度產物均可被加熱或冷卻。 尋求具備以下特點之熱交換器的具體實施態樣： •允許兼具短逗留時間及低失壓， •易於清潔， •易於製造， •易於密封， •可在大範圍的溫度、壓力及黏度下使用，及 •產物空間與加熱或冷卻空間之間的溫差易於處理。 本發明目的的達成係透過一在被產物塡充的管中具有 特殊設計的置換桿之管束熱交換器。該置換桿係設計成佔 據大於40%之管體積，較佳係佔據大於50%之管體積，且 非常特別佳地佔據大於60%之管體積。爲使裝置中之被產 物塡充的體積保持在少量，將一或多個置換體較佳地安置 於該裝置的熱交換器罩蓋中，或使用至少一個平板托盤。 【實施方式】 1 .管束熱交換器的設計 說明 管束熱交換器包含一殼體（4)及一管束，該管束係 由一或多個實質上平行排列的管所形成，且待調溫的產物 流經該管束。該些管可以齊平、互補或彼此爲管洞的同心 圓的方式排列。較佳係以最小及實貫上相等的管空間排列 201000844 ，如此而產生較小的產物塡充體積（6 )。管以同心圓方 式排列係特別佳地，藉此獲得朝向管之均勻流動及在底部 區域較少的死角。 產物流通過管並藉由套管加熱或冷卻。加熱或冷卻介 質（5)流穿過管之外部套殼。加熱或冷卻介質（5)可以 與產物流呈交錯流、逆流或順流的方式流向管子。較佳是 以交錯逆向流的方式實質上進行調溫，因爲調溫介質（5 )與產物空間（6 )之間的較小驅動溫度梯度因此而足夠 。爲使淨空可以一簡單的方法實施，產物較佳地由頂部向 底部流通過熱交換器。爲使加熱或冷卻介質（5)的除氣 能以一簡單的方法實施，調溫介質（5 )較佳地係由底部 向頂部流通過熱交換器。 管束之至少一端係利用一托盤圍住，而產物係藉由此 托盤產物進入或離開。該托盤可爲一具有薄壁的熱交換器 罩蓋（2 )型態或厚壁但緊密平板托盤（1 7 )之型態。該 托盤較佳具有一裝置凸緣，使其可以凸緣連接的方式連接 至該熱交換器之主體或可被再次移開。該托盤可具有一連 接件，其較佳位於軸上，且產物可由連接件進入或暴露。 在軸附近之數個可藉以暴露產物之連接件也可被想像到。 該托盤較佳地係設計成其可被調溫介質加熱或冷卻的方式 。然而，電子加熱也可被想像到。 熱交換器直接與另一裝置連接也可被想像到，使得對 應的托盤也可被配置於此端。 爲補償膨脹，若需要時可於外部套殼內使用一補償器 -8- 201000844 來補償管束與外部套殼間不同的熱膨月長 優點 對於相對高黏度產物，熱交換器管中的失壓可藉由選 擇合適管直徑加以控制。 2 .置換桿的設計 說明 爲降低熱交換管中產物體積（6)及增加熱轉移，置 換桿（7、10、12、15)係導入管中。置換桿（7、10、12 、15)可部分突入熱交換蓋（2)。置換桿（7、10、12、 15)設計成其可取代大於40 %的熱父換管體積的方式。較 佳地大於60 %的管中空體積被置換桿（7、10、I2、15)取 代。較佳地，少於9 5 %的體積被取代，以同時保持熱交換 器的緊密設計及少量失壓。置換桿（7、10、I2、15)的 外部輪廓係經設計成使置換桿（7、1 〇、1 2、1 5 )之軸位 於管之中心以避免死角及在熱交換器管截面得到均勻流量 。產物流流經置換桿（7、1 〇、1 2、1 5 )及熱交換器管內 壁之間的間隙（1 1 )。 爲使置換桿（7、1 0、1 2、1 5 )以界定的間隙位於管 的中心，置換桿（7、1 0、1 2、1 5 )可以設計成例如下列 方式： .兩端密封之中空或實心的管子（15) ’置換桿的截 面沿著軸向在至少兩個區域（1 4、1 6 )變形’以使其置於 -9 - 201000844 管（9 )之中心（參考第2圖及第5-6圖）， •兩端密封之中空或實心的管子（12)，在至少兩個 軸位置具有向外固定的元件（1 3 )，且使其置於管的中心 (參考第3-4圖）， •延著管軸搖擺並具有置換體積特性的平板。 置換桿（7、10、12、15)較佳地被推入管（9)中， 使其若需要可基於清潔或測試之目的而再次移除。置換桿 (7、10、12、15)也可包含數個依序連接的獨立桿。可 理解的是可利用塡滿可促進熱傳遞的介質之中空置換桿， 例如，其可含有在熱區被汽化及在冷區被冷凝的水使熱在 軸方向被傳遞。其同時也可被理解利用熱轉移介質流通過 置換管來轉移熱。進一步的可能包括使用電加熱的置換桿 ’其結果可使特定的熱轉移區域進一步增加且進一步降低 逗留時間。同樣地可想而知的是使用上述之置換桿的組合 〇 置換桿較佳地在管被加熱的部分產生狹窄的截面。在 注入區，增加截面可用於減少在管底部區域的失壓。 優點 置換桿（7、10、12、15)降低在導管（6)中產物的 逗留並增加特定的熱交換區域。在具有相同熱效能及管數 目的微熱交換器以及平板熱交換器的情況，穿過具置換桿 (7、1〇、12、15)之管束熱交換器的失壓是較小的。在 微熱交換器及平板熱交換器的情況中，失壓只有在實質上 -10- 201000844 增加這些類型的熱交換器中的管數目時才可被降低至具置 換桿之管束熱交換器的程度。小的管直徑及大的管數目使 得清潔這些熱交換器相當困難。 具置換桿的管束熱交換器的逗留時間當然短於不具相 同直徑置換桿的管束熱交換器。逗留時間只有在具有顯著 較小直徑的空管時可調整成與具置換桿之管束熱交換器的 相同程度，然而，其於是實質上是較長的。 3.熱交換器罩蓋中的置換體 說明 爲使在熱交換器罩蓋（2)中的逗留最小化，置換體 (3)係安裝於罩蓋（2)中，罩蓋（2)同樣可被加熱或 冷卻。爲使其置於中心，其可於例如其外側具有金屬片或 栓。爲使熱交換器管均勻裝塡液體，朝向熱交換器管之側 較佳爲圓錐狀；參考第7圖。 優點 在熱交換器罩蓋（2)中的較短逗留時間，且因此較 低的產物熱負載。 4.平板托盤 產物入口（ 1 )與產物出口（ 8 )的區域也可設計爲具 凹陷（低體積端）之平板托盤（17)(參考第8圖）。該 凹陷的尺寸是使產物在托盤中的逗留時間在完全塡充時介 -11 - 201000844 於〇 . 5秒至2 0秒’較佳地介於1 · 5秒至1 5秒，在部份塡充時 介於1秒至40秒’較佳地介於1.5秒至30秒。該凹陷可利用 例如車工或磨銑製造。該平板之凹陷可爲圓錐狀。 5 .操作參數 說明 操作溫度 T=-20°C至+4 0 0°C。 管中產物空間（6)及罩蓋（2)的壓力P=-0.95 bar g 至 + 1 00 barg 〇 在熱轉移介質（5 )之空間中的壓力可介於P == -0.95 barg至+50 barg。熱轉移介質（5)的溫度可爲τ = -201至 + 4 0 0 °C ° 熱轉移介質（5 )可以液態或氣態注入。 本發明描述之熱父換器係適合用於加熱或冷卻具有黏 S η =0.1 mPa.s 至 500 Pa. s之產物。產物於熱交換器之逗留 時間可爲1秒至3 0 0秒。 優點201000844 6. INSTRUCTIONS OF THE INVENTION: TECHNICAL FIELD OF THE INVENTION The present invention relates to a heat exchanger for temperature sensitive and/or polymerizable products. [Prior Art] The related literature discloses a plurality of different types of heat exchangers, and thus, for example, a heat exchanger type composed of a plate heat exchanger or a micro heat exchanger is suitable for a short stay time. However, such heat exchangers have the disadvantage of being due to narrow flow gaps, which are only suitable for low viscosity products. In the case of higher viscosity products, the loss of pressure throughout these heat exchangers can be very high. In the case where the product tends to polymerize, for example, a monomer or a polymer slurry still containing a monomer, there is a risk that the monomer will polymerize during or after the operation of the heat exchanger. It is very complicated to remove the polymerized slurry from the plate heat exchanger and the micro heat exchanger if not impossible. For high viscosities, especially kPas and high pressures above 1 Torr, no flat plate heat exchangers are available due to manufacturing methods and the forces generated. U.S. Patent No. 1,96,907 describes a tube bundle heat exchanger having a spiral groove displacement body in its tube. Due to its helical flow, a particularly efficient heat exchange is achieved. However, since the medium to be tempered flows in the displacement tube, additional pressure loss and extra residence time are generated, which may cause damage to the product. Further, complex designs also result in high cost, difficult to disassemble, and difficult clearance procedures. Germany - G 87 12 8 1 5 (VIA Gesellschaft fur Verfahrenstechnik) 201000844 A tube bundle heat exchanger for a compressed air dryer is described. To save material, the displacement body in the introduction tube sequentially contains a tube near the injection end. The displacement tube can have a grooved surface. However, because the trays that do not use very small hold-ups and the displacement rods are not close to the bottom, this design (not developed for temperature sensitive products) therefore has a large product charge volume. Moreover, this example of temperature sensitive polymers poses a major drawback due to the inability of the displacement tube to be disassembled. Germany DE-G 89 03 349 (VIA Gesellschaft fiir Verfahrenstechnik) discloses a tube bundle heat exchanger, in particular for a compressed air dryer. In order to allow the heat transfer medium to flow through the device as uniformly as possible, a perforated plate is provided in the device to ensure uniform flow to the tube. However, in this example of the tube bundle heat exchanger, heat transfer under mild conditions is not necessary, so there is no special requirement for the displacement rod section, and a replacement cap or plate tray with minimal embrittlement is not required. Further, the replacement rod cannot be removed. Heat exchangers that exhibit small loss of pressure in the case of relatively high viscosity products are common, such as tube bundle types. In this embodiment, the product flows through a plurality of tubes arranged in parallel. However, the disadvantage here is that the tube bundle heat exchanger typically has a small and special heat exchange space. This particular heat exchange space is defined herein as the ratio of the heat exchange area to the volume of the product in the tube. Because of this small heat exchange space, a heat exchanger having a relatively large amount of support in the tube is usually required. The residence time of the tube bundle heat exchanger is therefore very high. SUMMARY OF THE INVENTION In view of the foregoing prior art, it is an object of the present invention to develop a heat exchanger that allows the product to be heated in -6-201000844 or to be cooled to be as short as possible in the heat exchanger. The heat exchanger should be further designed such that low viscosity or higher viscosity products can be heated or cooled. Seek specific implementations of heat exchangers with the following features: • Allows for short residence times and low pressure loss, • Easy to clean, • Easy to manufacture, • Easy to seal, • Can be used over a wide range of temperatures, pressures and viscosities The temperature difference between the use and the product space and the heating or cooling space is easy to handle. The object of the present invention is achieved by a tube bundle heat exchanger having a specially designed displacement rod in a tube that is filled with product. The displacement rod is designed to occupy more than 40% of the tube volume, preferably more than 50% of the tube volume, and very particularly preferably occupy more than 60% of the tube volume. To maintain a small volume of product in the device, one or more of the displacement bodies are preferably disposed in the heat exchanger cover of the device, or at least one plate tray is used. [Embodiment] 1. Design of tube bundle heat exchanger The tube bundle heat exchanger comprises a casing (4) and a tube bundle formed by one or more substantially parallel arranged tubes, and to be tempered The product flows through the tube bundle. The tubes may be arranged flush, complementary or concentric with each other for the tube hole. It is preferred to arrange 201000844 with a minimum and a substantially uniform tube space, thus resulting in a smaller product charge volume (6). The tubes are particularly preferably arranged in a concentric manner whereby a uniform flow towards the tube and fewer dead spots in the bottom region are obtained. The product stream passes through the tube and is heated or cooled by a sleeve. The heating or cooling medium (5) flows through the outer casing of the tube. The heating or cooling medium (5) can flow to the tube in a staggered, countercurrent or downstream flow with the product stream. Preferably, the temperature adjustment is substantially performed in a staggered reverse flow manner because a smaller drive temperature gradient between the temperature control medium (5) and the product space (6) is therefore sufficient. In order for the headroom to be carried out in a simple manner, the product preferably flows from the top to the bottom through the heat exchanger. In order to carry out the degassing of the heating or cooling medium (5) in a simple manner, the temperature control medium (5) preferably flows from the bottom to the top through the heat exchanger. At least one end of the tube bundle is surrounded by a tray, and the product enters or leaves by the tray product. The tray can be of the form of a thin walled heat exchanger cover (2) or a thick wall but a tight plate tray (17). The tray preferably has a device flange that can be flanged to the body of the heat exchanger or can be removed again. The tray can have a connector that is preferably located on the shaft and the product can be accessed or exposed by the connector. Several connectors around the shaft that can be exposed to the product can also be imagined. The tray is preferably designed such that it can be heated or cooled by a temperature regulating medium. However, electronic heating can also be imagined. The connection of the heat exchanger directly to another device can also be imagined so that the corresponding tray can also be configured at this end. To compensate for the expansion, a compensator -8-201000844 can be used in the outer casing to compensate for the different thermal expansion between the bundle and the outer casing. If necessary, for a relatively high viscosity product, the pressure loss in the heat exchanger tube It can be controlled by selecting the appropriate tube diameter. 2. Design of the replacement rod In order to reduce the volume of the product in the heat exchange tube (6) and increase the heat transfer, the replacement rods (7, 10, 12, 15) are introduced into the tube. The displacement rods (7, 10, 12, 15) can partially protrude into the heat exchange cover (2). The displacement rods (7, 10, 12, 15) are designed in such a way as to replace the hot parent exchange volume by more than 40%. Preferably, more than 60% of the tube hollow volume is replaced by a displacement rod (7, 10, I2, 15). Preferably, less than 95% of the volume is replaced to maintain the tight design of the heat exchanger and a small amount of pressure loss. The outer contours of the displacement rods (7, 10, I2, 15) are designed such that the shaft of the displacement rod (7, 1 〇, 1 2, 1 5) is located at the center of the tube to avoid dead ends and is obtained in the heat exchanger tube section. Uniform flow. The product stream flows through the gap (1 1 ) between the displacement rods (7, 1 〇, 1 2, 1 5 ) and the inner wall of the heat exchanger tubes. In order to position the displacement rod (7, 10, 1, 2, 1 5) at the center of the tube with a defined gap, the displacement rods (7, 10, 1, 2, 15) can be designed, for example, in the following manner: Hollow or solid tube (15) 'The section of the displacement rod is deformed along the axial direction in at least two regions (1, 4, 16) to place it in the center of the -9 - 201000844 tube (9) (refer to 2 and 5-6), • A hollow or solid tube (12) sealed at both ends with an outwardly fixed element (13) at at least two axial positions and placed in the center of the tube ( Refer to Figure 3-4), • A plate that sways along the tube axis and has a displacement volume characteristic. The displacement rods (7, 10, 12, 15) are preferably pushed into the tube (9) so that they can be removed again for cleaning or testing purposes if desired. The displacement rods (7, 10, 12, 15) may also contain a plurality of independent rods that are sequentially connected. It will be appreciated that a hollow displacement rod that utilizes a medium that promotes heat transfer can be utilized, for example, it can contain water that is vaporized in the hot zone and condensed in the cold zone to transfer heat in the axial direction. It can also be understood that the heat transfer medium is used to transfer heat through the displacement tube. Further possibilities may include the use of electrically heated displacement rods' which result in a further increase in the specific heat transfer zone and further reduction in residence time. It is also conceivable that the combination of the above-described displacement rods 〇 displacement rods preferably produces a narrow cross section in the portion where the tubes are heated. In the injection zone, an increased cross section can be used to reduce the pressure loss in the bottom region of the tube. Advantages The displacement rods (7, 10, 12, 15) reduce the residence of the product in the conduit (6) and increase the specific heat exchange area. In the case of a micro heat exchanger having the same thermal efficiency and number of tubes and a plate heat exchanger, the pressure loss through the tube bundle heat exchanger having the displacement rods (7, 1〇, 12, 15) is small. In the case of micro heat exchangers and plate heat exchangers, the pressure loss can only be reduced to the extent of the tube bundle heat exchanger with displacement rods when the number of tubes in these types of heat exchangers is substantially increased by -10- 201000844 . The small tube diameter and large number of tubes make it relatively difficult to clean these heat exchangers. The tube bundle heat exchanger with the displacement rod has a shorter residence time than the tube bundle heat exchanger without the same diameter displacement rod. The residence time can be adjusted to the same extent as a tube bundle heat exchanger with a displacement rod only when it has a significantly smaller diameter tube, however, it is then substantially longer. 3. The replacement body in the heat exchanger cover is described as minimizing the stay in the heat exchanger cover (2), and the replacement body (3) is attached to the cover (2), and the cover (2) is also Can be heated or cooled. To center it, it may have, for example, a metal sheet or peg on its outer side. In order to uniformly charge the heat exchanger tubes, the side facing the heat exchanger tubes is preferably conical; see Figure 7. Advantages Shorter residence time in the heat exchanger cover (2), and therefore lower product heat load. 4. Plate tray The area of the product inlet (1) and product outlet (8) can also be designed as a flat tray (17) with a recessed (low volume end) (refer to Figure 8). The size of the recess is such that the product stays in the tray during the full charge period - -11 - 201000844 〇. 5 seconds to 20 seconds 'better between 1.25 seconds and 15 seconds, in part The charge time ranges from 1 second to 40 seconds', preferably between 1.5 seconds and 30 seconds. The recess can be manufactured, for example, by lathe or milling. The depression of the plate may be conical. 5. Operating parameters Description Operating temperature T=-20°C to +4 0 0°C. The pressure in the product space (6) and the cover (2) in the tube P=-0.95 bar g to + 1 00 barg 〇 The pressure in the space of the heat transfer medium (5) can be between P == -0.95 barg to + 50 barg. The temperature of the heat transfer medium (5) can be τ = -201 to + 40 ° C. The heat transfer medium (5) can be injected in a liquid or gaseous state. The hot parent converter described in the present invention is suitable for heating or cooling a product having a viscosity of S η = 0.1 mPa·s to 500 Pa·s. The product can stay in the heat exchanger for a period of from 1 second to 300 seconds. advantage
、壓力及黏度爲可 與先前技術之傳統熱交換器及 比較 具有環狀間隙之熱交換器的 以下表格總結了管與環Μ 間隙中之質能平衡及流量和 -12- 201000844 熱轉移的計算之結果。失壓的計算係基於具有層流（ Hagen-Poiselle流）的管或具有層流的環狀間隙的脈衝守 恆方程式的分析結果。轉換計算係基於流體力學及熱未形 成的層流之半經驗紐塞（N u s s e 11 )値關係。除非特別指明 ’假設質量流1 〇〇〇 kg/h ’在管中的60秒逗留時間，待加熱 的介質溫度增加100K，及一介於熱轉移介質（5)及待加 熱的介質之間的溫度差對數爲30K。末二數値可結合而得 商3.33。更進一步地’材料値使用〇·ΐ5 W/mK的導熱率、 1 000 kg/m3的密度，2200 j/kgK的比熱容，及1 pa.s之恆定 動力黏度，即假設爲牛頓流體。更進一步地，其係假設在 熱轉移側的熱傳抗性及穿過管壁的傳導抗性可以被忽略。 管，例A 管，例B 管，例C 管，例D 管，例E 管，例F 管，例G 管，例Η 環狀間 隙，例I 逗留時間/S 60 25 60 580 60 5 60 60 60 溫度增加 與溫度差 對的商 3.33 3.33 12.7 3.33 0.80 3.33 23.7 3.33 3.33 失壓/bar 4.4 4.4 4.4 4.4 4.4 4.4 4.4 0.069 4.4 管的數目 170 408 2120 18 6 2041 6610 1360 40 管長/m 4.7 2.0 2.0 45.5 14.6 0.4 1.4 0.6 3.0 管直徑/mm 5.2 3.3 2.2 16 16 1.5 1.5 5.2 24/20 實例A展示傳統管束熱交換器，需要非常細長管以達 到指定的條件。然而，其製造不僅非常困難且實際上難以 清潔。 實例B及C展示較短管之較短的逗留時間（實例B)或 -13- 201000844 被改變的熱環境（實例c)的可能。然而同一時間，管货 徑不再降低及管數目明顯的增加，所以其無法作爲實例a 的替代方案。 實例D及E展示可藉由較長的逗留時間（實例〇)或較 高壁溫度（因較大的溫度差對數，實例E )而得到較大的 管直徑。然而’由於較大直徑所致之較佳可清潔性的優 被極度增加的管長過度補償，致使製造變得非常困難，且 因逗留時間及壁溫的增加造成產物品質的惡化。進一步％ ’在建物中如此長的裝置也是有問題的。 實例F及G展示較小管直徑，藉由較小逗留時間（實例 F)或改變的熱條件（實例G )，導致極大數目的管。由管 束裝置將需暴露於高壓及高溫的觀點而言此一大數目的，細 管無法被製造。 無法忽略的管長更是不允許清潔該裝備內部。 實例Η展示因增加管的數目及較短的管長所導致的失 壓減低並不會導致較小的管直徑。由於具有無法忽略的長 度之大數目的薄管，此處也使清潔如同製造性差不多是不 可能的。 根據本發明的設計（實例I )與傳統管束熱交換器（ 實例A-Η)之比較： 實例I經由實施例展示了本發明之具有置換桿的熱交 換器的設計。考慮逗留時間、熱條件及失壓，相較於傳統 熱交換器（實例A-Η )，其具有非常大的管直徑，確保適 合清潔的可能。此外，相較於實例A、D及Ε，管長係保持 -14- 201000844 在範圍內，使其結果允許有良好可製造性及可清潔性且僅 需小空間。更進一步地與實例Α-C及F-H相比較，管的數目 係小的，使得簡單及經濟的製造因而變成可能。 本發明之管束熱交換器使用於聚合物的合成可特別地 具優勢，因其短的逗留時間並結合有效的熱轉移，使產物 有小的熱負載，因此可預防非所欲的聚合反應。 計算的方法 由管壁的熱平衡 ~d^ )' Pcp ATS = — ^ A -TrdaL-AT, T 4 dh 及指定三個幾何參數（外部間隙直徑心，內部間隙直徑 A，管長L )中的兩個可計算第3個幾何參數。 此處爲管或環狀間隙的長度，τ係爲逗留時間，A係 爲外部間隙直徑或管直徑，6係爲環狀間隙的內部直徑（ 管：A = 0 ) ’ p係爲密度，係爲比熱容，」係爲漿料的 增加溫度’係爲心水力直徑，Α係爲導熱率，J〜係爲加熱 的介質（5)與漿料的溫度差對數値。 管之平均紐塞數的計算係根據Baehr/Stefan ( Heat and Mass Transfer, Springer-V erlag Berlin, 1 994, pages 381-382) ’考量流體力學及熱力學起動値，使用下列程 式而計算： Nu„ * m，tube 3.657, Pressure and Viscosity The following table, which compares the conventional heat exchangers of the prior art with those of a heat exchanger with an annular gap, summarizes the mass balance and flow in the gap between the tube and the ring and the calculation of the heat transfer from -12 to 201000844 The result. The calculation of the loss of pressure is based on the analysis of a pulse-conservative equation with a laminar flow (Hagen-Poiselle flow) or an annular gap with laminar flow. The conversion calculation is based on the semi-employed Neux (N u s s e 11 )値 relationship of fluid mechanics and heat unformed laminar flow. Unless specifically specified as 'hypothetical mass flow 1 〇〇〇kg/h' 60 seconds in the tube, the temperature of the medium to be heated is increased by 100K, and a temperature between the heat transfer medium (5) and the medium to be heated The difference logarithm is 30K. The last two numbers can be combined to obtain 3.33. Furthermore, the material 値 uses 导热·ΐ5 W/mK thermal conductivity, density of 1 000 kg/m3, specific heat capacity of 2200 j/kgK, and constant dynamic viscosity of 1 pa.s, which is assumed to be Newtonian fluid. Further, it is assumed that heat transfer resistance on the heat transfer side and conduction resistance through the tube wall can be ignored. Tube, Case A, Case B, Case C, Case D, Case E, Case F, Case G, Example 环状 Annular clearance, Example I Stay time / S 60 25 60 580 60 5 60 60 60 quotient of temperature increase and temperature difference pair 3.33 3.33 12.7 3.33 0.80 3.33 23.7 3.33 3.33 Pressure loss /bar 4.4 4.4 4.4 4.4 4.4 4.4 4.4 0.069 4.4 Number of tubes 170 408 2120 18 6 2041 6610 1360 40 Tube length / m 4.7 2.0 2.0 45.5 14.6 0.4 1.4 0.6 3.0 Tube diameter/mm 5.2 3.3 2.2 16 16 1.5 1.5 5.2 24/20 Example A shows a conventional tube bundle heat exchanger that requires a very slender tube to achieve the specified conditions. However, its manufacture is not only very difficult but actually difficult to clean. Examples B and C show the possibility of a shorter residence time for a shorter tube (Example B) or -13-201000844 for a changed thermal environment (Example c). At the same time, however, the pipe diameter is no longer reduced and the number of pipes is significantly increased, so it cannot be used as an alternative to example a. Examples D and E show larger tube diameters by longer residence time (example 〇) or higher wall temperatures (due to larger temperature difference log, example E). However, the superior cleanability due to the larger diameter is excessively compensated by the extremely increased tube length, which makes the production extremely difficult, and the deterioration of the product quality due to the increase in the residence time and the wall temperature. Further % 'the construction of such a long device is also problematic. Examples F and G show smaller tube diameters, resulting in a very large number of tubes with a smaller residence time (Example F) or altered thermal conditions (Example G). A large number of thin tubes cannot be manufactured from the viewpoint that the tube bundle device is exposed to high pressure and high temperature. The length of the tube that cannot be ignored is not allowed to clean the inside of the equipment. The example shows that the reduction in pressure loss due to the increased number of tubes and the shorter tube length does not result in a smaller tube diameter. Due to the large number of thin tubes having a length that cannot be ignored, it is also impossible to make cleaning as manufacturous here. Comparison of a design according to the invention (Example I) with a conventional tube bundle heat exchanger (Example A-Η): Example I illustrates, by way of example, a design of a heat exchanger with a displacement rod of the present invention. Considering the length of stay, thermal conditions and loss of pressure, it has a very large tube diameter compared to conventional heat exchangers (Example A-Η), ensuring the possibility of cleaning. In addition, compared to Examples A, D, and Ε, the tube length was maintained in the range of -14-201000844, allowing the results to allow for good manufacturability and cleanability with only a small space. Further in comparison with the examples Α-C and F-H, the number of tubes is small, making it possible to manufacture simply and economically. The use of the tube bundle heat exchanger of the present invention for the synthesis of polymers is particularly advantageous because of its short residence time combined with effective heat transfer, which results in a small thermal loading of the product, thereby preventing undesired polymerization. The calculation method consists of the thermal equilibrium of the tube wall ~d^)' Pcp ATS = — ^ A -TrdaL-AT, T 4 dh and two of the three geometric parameters (outer gap diameter core, internal gap diameter A, tube length L) The third geometric parameter can be calculated. Here is the length of the tube or annular gap, τ is the residence time, A is the external gap diameter or tube diameter, and 6 is the internal diameter of the annular gap (tube: A = 0) 'p is the density, For the specific heat capacity, the "increased temperature of the slurry" is the heart hydraulic diameter, the lanthanum is the thermal conductivity, and the J is the temperature difference between the heated medium (5) and the slurry. The calculation of the average Nusselt number of the tube is calculated according to Baehr/Stefan (Heat and Mass Transfer, Springer-Verlag Berlin, 1 994, pages 381-382) 'Consideration of fluid mechanics and thermodynamic starting 値, using the following formula: Nu„ * m,tube 3.657
tanh(2_432-/V1/3)X]/6 [ tanh(2.264-Z1/3 +X.1-X 0.0499 2/3 tanh(jf) -15- 201000844 此處Pr係爲普蘭特値且X係爲非因次長度： ^ L τλ ~ dhPe d] p cp 加上A：=心/A，進一步得到被加熱的外部環狀間隙中 的平均紐塞値，如下式所示： Μ/—=3.657 + 1.2·火1/2+(他„ ,*-3.657).(1 + 0.14.火,/3 ) 根據 Martin ( WSrmetibertrager [Heat exchangers], Georg Thieme Verlag Stuttgart, 1 98 8, page 24) ’ 以下適 合於表示環狀間隙或管（尤=〇 )中的失壓： Δρ = 32 μ ύ \-Κ2 1-欠4 + 1η⑻ 【圖式簡單說明】 第1圖展示熱交換器管之截面。 第2、5及6圖展示本發明之管的一具體實施態樣。 第3及4圖展示本發明之管的另一具體實施態樣。 第7圖係爲本發明面向熱交換器管之側的一具體實施 態樣。 第8圖係爲本發明之熱交換器中平板托盤的一具體實 施態樣。 -16 -Tanh(2_432-/V1/3)X]/6 [ tanh(2.264-Z1/3 +X.1-X 0.0499 2/3 tanh(jf) -15- 201000844 where Pr is Plant and X For the non-dimensional length: ^ L τλ ~ dhPe d] p cp plus A:= heart / A, further obtain the average New Zealand 中 in the heated outer annular gap, as shown in the following formula: Μ / - = 3.657 + 1.2·Fire 1/2+ (He „ ,*-3.657).(1 + 0.14.Fire, /3) According to Martin (WSrmetibertrager [Heat exchangers], Georg Thieme Verlag Stuttgart, 1 98 8, page 24) ' It is suitable for indicating the pressure loss in the annular gap or tube (especially = 〇): Δρ = 32 μ ύ \-Κ2 1- under 4 + 1η(8) [Simplified illustration] Figure 1 shows the cross section of the heat exchanger tube. 2, 5 and 6 show a specific embodiment of the tube of the present invention. Figures 3 and 4 show another embodiment of the tube of the present invention. Fig. 7 is a side of the present invention facing the heat exchanger tube A specific embodiment of the present invention is shown in Fig. 8. Fig. 8 is a specific embodiment of the flat tray in the heat exchanger of the present invention.