SO2氧化反应为放热反应，通常在气——固反应床中进行。由于反应升温达到平衡线，将不能继续进行反应，故通常是每经一段绝热反应后将气体冷却，再作下一段反应，反应一般分若干段进行。现有的具有内部换热结构的气体固定床反应器型式有几种，如：申请号为：CN2290400的中国专利为改进均温型气固相催化反应器；申请号为CN2288770的中国专利为一种放热气-固相催化合成反应器；申请号为：CN1174096的中国专利为一种接近最佳温度的催化反应改进工艺及其合成反应器；申请号为：CN85100111A的中国专利为在列管式固定床反应器中进行催化反应的方法及装置；申请号为：CN85204137U的中国专利为对向流低阻力催化反应器；申请号为：CN1225850的中国专利为用于催化反应的固定床反应器。但上述几种气体转化器的内部换热结构都存在着同样的缺点：一是采用管式换热结构，传热系数低，难以实现有效的传热强化；二是冷热流是以非全逆流形式换热，有效传热温差小。由于以上两方面的缺点，导致现有的SO2气体转化器内部换热面积大，耗材多，设备造价高，而且体积庞大，安装与维修都不方便。此外，由于以上设备结构的缺点，使得转化器仅限于4～5段转化反应，转化过程中的平均反应温度较低导致SO2氧化反应速率低，所需催化剂用量多，设备投资高。The SO2 oxidation reaction is an exothermic reaction, usually carried out in a gas-solid reaction bed. Since the temperature of the reaction reaches the equilibrium line, the reaction cannot be continued. Therefore, the gas is usually cooled after each stage of adiabatic reaction, and then the next stage of reaction is performed. The reaction is generally carried out in several stages. There are several types of existing gas fixed bed reactors with internal heat exchange structure, such as: the application number is: the Chinese patent of CN2290400 is an improved uniform temperature gas-solid phase catalytic reactor; the application number is the Chinese patent of CN2288770 is a A kind of exothermic gas-solid-phase catalytic synthesis reactor; the application number is: the Chinese patent of CN1174096 is a kind of catalytic reaction improvement process and its synthesis reactor close to the optimum temperature; A method and device for catalytic reaction in a fixed-bed reactor; the Chinese patent with application number CN85204137U is a counterflow low-resistance catalytic reactor; the Chinese patent with application number CN1225850 is a fixed-bed reactor for catalytic reactions. However, the internal heat transfer structures of the above-mentioned gas converters all have the same disadvantages: first, the tube heat transfer structure is adopted, and the heat transfer coefficient is low, so it is difficult to achieve effective heat transfer enhancement; Countercurrent heat exchange, the effective heat transfer temperature difference is small. Due to the shortcomings of the above two aspects, the existingSO2 gas converter has a large internal heat exchange area, many consumables, high equipment cost, large volume, and inconvenient installation and maintenance. In addition, due to the shortcomings of the above equipment structure, the converter is limited to 4-5 stages of conversion reaction, the average reaction temperature in the conversion process is low, resulting in a lowSO2 oxidation reaction rate, a large amount of catalyst required, and high equipment investment.
本发明的目的就是为了解决和克服现有SO2气体转化器内部换热结构存在的管式换热传热系数低，难于实现传热强化，冷热流非全逆流换热，即错流换热，有效传热温差小、导致体积大、安装维修不方便、耗材多、造价高、以及转化反应段数太少，转化平均反应温度较低，导致氧化反应速率低、催化剂耗量大、投资大等的问题和缺点，研究发明一种具有高效强化传热性能的内部换热结构、可较大幅度提高传热系数，并实现冷热流全逆流换热，提高有效传热温差，可使转化段数扩展到10段以上，有效提高转化过程中的平均反应温度，增大SO2氧化反应速率，大幅减少催化剂用量，节省设备投资，缩小设备体积，安装维修方便的板翅式内部移热SO2氧化固定床反应器。The purpose of the present invention is to solve and overcome the low heat transfer coefficient of tubular heat transfer existing in the internal heat transfer structure of the existingSO2 gas converter, it is difficult to achieve heat transfer enhancement, and the cold and hot flows are not fully countercurrent heat exchange, that is, cross flow exchange Heat, the effective heat transfer temperature difference is small, resulting in large volume, inconvenient installation and maintenance, many consumables, high cost, and too few conversion reaction stages, the average conversion reaction temperature is low, resulting in low oxidation reaction rate, large catalyst consumption, and large investment In order to solve the problems and disadvantages of such problems, we researched and invented an internal heat transfer structure with high-efficiency and enhanced heat transfer performance, which can greatly improve the heat transfer coefficient, and realize the full countercurrent heat transfer of cold and hot flows, improve the effective heat transfer temperature difference, and make the conversion The number of stages is extended to more than 10 stages, effectively increasing the average reaction temperature during the conversion process, increasing the reaction rate of SO2 oxidation, greatly reducing the amount of catalyst, saving equipment investment, reducing equipment volume, and easy installation and maintenance. Plate-fin internal heat transfer SO2 Oxidation fixed bed reactor.
本发明是通过下述技术方案来实现的，本板翅式内部移热SO2氧化固定床反应器的结构示意图如图1所示，其A-A向视图如图2所示；其连续平翅片横向板翅设置示意图如图3所示；其连续平翅片纵向板翅设置示意图如图4所示；其非连续裂齿状翅片形状示意图如图5所示。本反应器由多块纵向金属板把反应器内部分割为多层相邻的SO2原料气冷体流道与SO3反应气热体流道，反应器壳体与多块纵向金属板构成等距平行纵向流道，冷热流体流道相间交错设置，SO3热流道沿纵向设置多段催化剂填料层，每相邻两段催化剂填料层中设置散热板翅及限流边框，对应冷流道侧面也设置加热板翅、冷热流道与回流联箱构成流道回路，相隔两段催化剂填料层之间是板翅冷却面，每段催化剂填料层后均紧接一段板翅冷却面，使在反应器矩形壳体内构成多通道板翅式内部移热固定床反应装置；它主要由反应器壳体1、纵向金属隔板2、催化剂填料层3、SO2冷流道加热翅片4、SO3热流道散热翅片5、催化剂填料层边框栅栏6、限流边框7及回流联箱8共同连接构成，其相互连接关系为：在反应器矩形壳体1内，多块纵向金属隔板2平行排列构成SO2冷流道9与SO3热流道10，在SO3热流道10中，由多块栅栏6与纵向金属隔板2相接构成催化剂段，内装填催化剂填料层3，由限流边框7及纵向金属隔板2上焊接的散热翅片5构成SO3的冷却通道紧接催化剂填料层3，在SO3冷却通道的对应侧面，由纵向金属隔板2与加热翅片4焊接构成SO2的加热通道，回流联箱8安置在反应器壳体1的顶端构成空腔回流区；散热翅片5与加热翅片4是纵向水平翅片或是横向垂直翅片，翅片是连续平翅片或是非连续裂齿状翅片。其动作原理如下：SO2原料气由冷流道9进入反应器壳体1，沿纵向金属隔板2流道流动，经加热翅片4加热升温至反应起燃温度，再经回流联箱8进入SO3反应器热流流道10，经催化剂填料层3反应后气温升高，通过散热翅片5移去热量，降低反应气温度，再进入下一段催化剂填料层继续反应，直到经最后一段催化剂填料层后流出反应器壳体1，原料气SO2与反应气SO3在反应器壳体1达到自热平衡。The present invention is achieved through the following technical solutions, the structural representation of the plate-fin type internal heat transfer SOOxidation fixed bed reactor as shown in Figure 1, its AA to view as shown in Figure 2; its continuous flat fins The schematic diagram of the horizontal plate-fin arrangement is shown in Figure 3; the schematic diagram of the longitudinal plate-fin arrangement of the continuous flat fins is shown in Figure 4; the shape diagram of the discontinuous split-toothed fins is shown in Figure 5. The reactor consists of multiple longitudinal metal plates that divide the interior of the reactor into multi-layer adjacent SO2 raw material gas cooling body flow channels and SO3 reaction gas heating body flow channels, and the reactor shell is composed of multiple vertical metal plates, etc. From the parallel longitudinal flow channels, the hot and cold fluid flow channels are arranged alternately, and the SO3 hot runner is provided with multi-stage catalyst packing layers along the longitudinal direction, and each adjacent two-stage catalyst packing layer is provided with heat dissipation plate fins and flow limiting frames, corresponding to the side of the cold runner Heating plate fins, hot and cold runners and return flow headers are also set to form a flow path circuit. There is a plate-fin cooling surface between two catalyst packing layers. Each catalyst packing layer is followed by a plate-fin cooling surface. The rectangular shell of the reactor constitutes a multi-channel plate-fin internal heat transfer fixed bed reaction device; it mainly consists of a reactor shell 1, avertical metal partition 2, a catalyst packing layer 3, a SO2 coldrunner heating fin 4, and a SO3 Thecooling fins 5 of the hot runner, theframe fence 6 of the catalyst packing layer, the current limitingframe 7 and the return header 8 are jointly connected and constituted. Parallel arrangement constitutes theSO2 cold runner 9 and theSO3 hot runner 10. In theSO3 hot runner 10, a plurality offences 6 andvertical metal partitions 2 are connected to form a catalyst section, and a catalyst packing layer 3 is filled inside. The heat dissipation fins 5 welded on theflow frame 7 and the longitudinalmetal partition plate 2 form the cooling channel of SO3 next to the catalyst packing layer 3, and on the corresponding side of the SO3 cooling channel, the longitudinalmetal partition plate 2 and theheating fin 4 are welded Constitute theSO2 heating channel, the reflux header 8 is placed on the top of the reactor shell 1 to form the cavity reflux area; thecooling fins 5 and theheating fins 4 are vertical horizontal fins or horizontal vertical fins, and the fins are Continuous flat fins or discontinuous split tooth fins. Its action principle is as follows: SO2 raw material gas enters the reactor shell 1 from the cold runner 9, flows along thelongitudinal metal partition 2 flow channel, heats up to the reaction ignition temperature through theheating fin 4, and then passes through the reflux header 8 Enter the hot flow channel 10 of theSO3 reactor, and the temperature rises after being reacted by the catalyst packing layer 3, and the heat is removed through thecooling fins 5 to reduce the temperature of the reaction gas, and then enter the next catalyst packing layer to continue the reaction until the last catalyst The packing layer flows out of the reactor shell 1, and the raw material gas SO2 and the reaction gas SO3 reach self-heating equilibrium in the reactor shell 1.
本发明与现有的技术相比，具有如下的优点和有益效果：(1)SO2冷流与SO3热流的对流换热在本反应器结构中是全逆流换热，有效传热温差高，克服了现有技术中冷热流体错流换热，有效传热温差低的缺点；(2)本反应器采用板翅式换热结构，可大大强化冷热流两侧的对流传热，克服了现有技术中管式换热结构传热效率低的缺点，总传热系数可增大2～3倍；(3)由于本反应器结构便于设置多级转化段(10级以上)，可有效提高反应过程的平均温度，增大反应速率，节省催化剂用量可达25～30％，大幅降低反应设备投资，同时也可降低气阻，节省操作费用；(4)本发明缩小了反应器设备体积，减少系统占地面积，方便设备的安装和维修。Compared with the prior art, the present invention has the following advantages and beneficial effects: (1) The convective heat exchange ofSO2 cold flow andSO3 hot flow is full countercurrent heat exchange in this reactor structure, and the effective heat transfer temperature difference is high , which overcomes the disadvantages of cross-flow heat exchange between hot and cold fluids in the prior art and low temperature difference in effective heat transfer; (2) The reactor adopts a plate-fin heat exchange structure, which can greatly strengthen the convective heat transfer on both sides of the hot and cold flow, It overcomes the disadvantage of low heat transfer efficiency of the tubular heat exchange structure in the prior art, and the total heat transfer coefficient can be increased by 2 to 3 times; (3) Since the reactor structure is convenient for setting multi-stage conversion sections (above 10 stages), The average temperature of the reaction process can be effectively improved, the reaction rate can be increased, the amount of catalyst can be saved by up to 25-30%, the investment of reaction equipment can be greatly reduced, and the air resistance can also be reduced at the same time, so as to save operating costs; (4) the present invention reduces the size of the reactor The size of the equipment reduces the area occupied by the system and facilitates the installation and maintenance of the equipment.
本发明的实施方式较为简单，可采用普通的板金工艺和机加工方法及设备即可加工。实施本发明，只要按图1～5所示设计、加工本装置的各部件，并按上面说明书所述的相互连接关系进行连接装配构成图1所示的流道结构，便能较好地实施本发明。例如，发明人推荐设计由8块厚5mm的纵向钢板在反应器中等距分隔出4个50mm宽的SO2冷道流与500mm宽的SO3热流道，3000mm的壳体高度，2200mm的壳体宽度，5000mm壳体纵向长度，SO3热流道中设置10段催化剂层，冷热流道的板翅均取20×3mm翅片，翅化率取3。The embodiment of the present invention is relatively simple, and can be processed by adopting ordinary sheet metal technology and machining methods and equipment. To implement the present invention, as long as each part of the device is designed and processed as shown in Figures 1 to 5, and connected and assembled according to the interconnection relationship described in the above specification to form the flow channel structure shown in Figure 1, it can be implemented better this invention. For example, the inventor recommends designing four 50mm wideSO2 cold runners and 500mm wideSO3 hot runners in the reactor equidistantly separated by 8 longitudinal steel plates with a thickness of 5mm, a shell height of 3000mm, and a shell of 2200mm Width, longitudinal length of 5000mm shell, 10 stages of catalyst layers in SO3 hot runner, plate fins of cold and hot runners are 20×3mm fins, finning rate is 3.
