CN1091392C

CN1091392C - Finned fixed-bed reactor with internal heat transfer for oxidizing SO2

Info

Publication number: CN1091392C
Application number: CN00117570A
Authority: CN
Inventors: 邓先和; 张亚君
Original assignee: South China University of Technology SCUT
Current assignee: South China University of Technology SCUT
Priority date: 2000-10-31
Filing date: 2000-10-31
Publication date: 2002-09-25
Anticipated expiration: 2020-10-31
Also published as: CN1300637A

Abstract

The present invention relates to a plate-fin type fixed bed reactor with internal heat transfer for oxidizing SO2, and equidistant parallel longitudinal flow channels are composed of multiple layers of longitudinal metal plates with plate fins and a casing, and hot and cold flow channels are staggered. The hot flow channels are lengthwise provided with multiple catalyst stuffing layers; heat radiation plate fins and current limiting frames are arranged between every two adjacent catalyst stuffing layers. The plate-fin type fixed bed reactor is mainly composed of the converter casing, the hot and cold flow channels separated by the longitudinal metal plates, the multiple catalyst layers, the plate fins of the hot and cold flow channels between the catalyst layers, and a flow channel loop composed of reflux collecting boxes and the hot and cold flow channels. The present invention has the advantages of strengthening heat transfer through gas reaction, saving catalyst dosage, reducing operation air resistance and equipment volume and decreasing equipment material consumption and investment.

Description

Plate-fin internal heat transfer SO 2The oxidation fixed bed reactors

The present invention is plate-fin internal heat transfer SO ₂The gas cyaniding fixed bed reactors claim gas converter again, belong to the augmentation of heat transfer technology, particularly the gas fixed bed reaction equipment of internal heat transfer structure.

SO ₂Oxidation reaction is exothermic reaction, Gu usually at gas---carry out in the reaction bed.Because reaction heats up and to reach balanced line, can not proceed reaction, so normally every after one section adiabatic reaction with gas cooled, remake next section reaction, reaction generally branch plurality of sections is carried out.Existing gas fixed bed reactors pattern with inner heat exchange structure has several, as: application number is: the Chinese patent of CN2290400 is for improving the homogeneous temperature type gas solid catalytic reactor; Application number is that the Chinese patent of CN2288770 is a kind of gas-solid phase exothermic catalytic synthesis reactor; Application number is: the Chinese patent of CN1174096 is that a kind of catalytic reaction near optimum temperature is improved technology and synthesis reactor thereof; Application number is: the Chinese patent of CN85100111A is for carrying out the method and the device of catalytic reaction in calandria type fixed bed reactor; Application number is: the Chinese patent of CN85204137U is a counter current flow lower resistance catalytic reactor; Application number is: the Chinese patent of CN1225850 is the fixed bed reactors that are used for catalytic reaction.But the inside heat exchange structure of above-mentioned several gas converters all exists same shortcoming: the one, adopt the pipe type heat transfer structure, and heat transfer coefficient is low, is difficult to realize effectively heat conduction reinforced; The 2nd, hot and cold stream is with the heat exchange of non-full adverse current form, and effectively heat transfer temperature difference is little.Because the shortcoming of above two aspects causes existing SO ₂The inner heat exchange area of gas converter is big, and consumptive material is many, the equipment manufacturing cost height, and also bulky, I﹠M is all inconvenient.In addition, because the shortcoming of above device structure makes converter only limit to 4～5 sections conversion reactions, the low SO that causes of the average reaction temperature in the conversion process ₂Oxidizing reaction rate is low, and required catalyst amount is many, the equipment investment height.

Purpose of the present invention is exactly to have SO now in order to solve and to overcome ₂The pipe type heat transfer heat transfer coefficient that the inner heat exchange structure of gas converter exists is low, be difficult to realize heat conduction reinforced, the non-full countercurrent flow of hot and cold stream, it is the cross-flow heat exchange, effectively heat transfer temperature difference is little, cause volume big, the installation and maintenance inconvenience, consumptive material is many, the cost height, and the conversion reaction hop count very little, it is lower to transform average reaction temperature, cause oxidizing reaction rate low, the catalyst consumption is big, big problem and the shortcoming that waits of investment, a kind of inside heat exchange structure of research invention with efficient augmentation of heat transfer performance, can improve heat transfer coefficient by a relatively large margin, and the full countercurrent flow of realization hot and cold stream, improve effective heat transfer temperature difference, the conversion hop count is expanded to more than 10 sections, effectively improve the average reaction temperature in the conversion process, increase SO ₂Oxidizing reaction rate significantly reduces catalyst amount, saves equipment investment, the reduction equipment volume, and installation and maintenance are plate-fin internal heat transfer SO easily ₂The oxidation fixed bed reactors.

The present invention realizes by following technical proposals, this plate-fin internal heat transfer SO ₂The structural representation of oxidation fixed bed reactors as shown in Figure 1, its A-A is to view as shown in Figure 2; Its continuous flat fin transverse plate wing is provided with schematic diagram as shown in Figure 3; The vertical plate wing of its continuous flat fin is provided with schematic diagram as shown in Figure 4; Its discontinuous carnassial tooth shape fin shape schematic diagram as shown in Figure 5.This reactor is divided into the adjacent SO of multilayer to inside reactor by polylith longitudinal metal plate ₂Raw material air cooling body runner and SO ₃Reaction gas hot body runner, reactor shell and polylith longitudinal metal plate constitute the vertical runner of equidistant parallel, and the cold fluid and hot fluid runner is alternate to be crisscross arranged SO ₃Hot flow path longitudinally is provided with multistage catalyst filling layer, in every adjacent two-stage catalytic agent packing layer heat sink wing and current limliting frame are set, corresponding cold runner side also is provided with heating plate wing, cold-hot flow passage and return header and constitutes the runner loop, be separated by between the two-stage catalytic agent packing layer is plate wing cooling surface, all be right after one section plate wing cooling surface behind every section catalyst filling layer, make in the reactor rectangular case, to constitute multichannel plate-fin internal heat transfer fixed-bed reactor; It is mainly by reactor shell 1, longitudinal metal dividing plate 2, catalyst filling layer 3, SO ₂Cold runner heating fin 4, SO ₃Hot runner cooling fin 5, catalyst filling layer frame fence 6, current limliting frame 7 and return header 8 connect and compose jointly, and its interconnected relationship is: in reactor rectangular case 1, polylith longitudinal metal dividing plate 2 is arranged in parallel and constitutes SO ₂Cold runner 9 and SO ₃Hot flow path 10 is at SO ₃In the hot flow path 10, being joined by polylith fence 6 and longitudinal metal dividing plate 2 constitutes catalyst section, and interior loading catalyst packing layer 3 constitutes SO by the radiating fin 5 of welding on current limliting frame 7 and the longitudinal metal dividing plate 2 ₃The cooling duct be right after catalyst filling layer 3, at SO ₃The corresponding side surface of cooling duct constitutes SO by longitudinal

metal dividing plate

2 and 4 welding of heating fin ₂Heat tunnel, the top that return header 8 is placed in reactor shell 1 constitutes the cavity recirculating zone; Radiating fin 5 is vertical equity fin or horizontal vertical fins with heating fin 4, and fin is continuous flat fin or discontinuous carnassial tooth shape fin.Its operating principle is as follows: SO ₂Unstripped gas enters reactor shell 1 by cold runner 9, and longitudinally metal partion (metp) 2 flow passage to reacting initiation temperature, enter SO through return header 8 through heating fin 4 heat temperature raisings again ₃Reactor hot-fluid runner 10, temperature raises after 3 reaction of catalyst filling layer, removes heat by radiating fin 5, reduce the reaction gas temperature, enter next section catalyst filling layer again and continue reaction, up to outflow reactor housing 1 behind final stage catalyst filling layer, unstripped gas SO ₂With reaction gas SO ₃Reach autothermal equilibrium in reactor shell 1.

The present invention has following advantage and beneficial effect compared with prior art: (1) SO ₂Cold flow and SO ₃The heat convection of hot-fluid is full countercurrent flow in this structure of reactor, and effectively the heat transfer temperature difference height has overcome cold fluid and hot fluid cross-flow heat exchange in the prior art, effectively the low shortcoming of heat transfer temperature difference; (2) this reactor adopts the plate fin heat-exchanging structure, can strengthen the convection heat transfer' heat-transfer by convection of hot and cold stream both sides greatly, has overcome the inefficient shortcoming of pipe type heat transfer structural thermal in the prior art, and overall heat-transfer coefficient can increase 2～3 times; (3) because this structure of reactor is convenient to be provided with multistage conversion zone (more than 10 grades), can effectively improve the mean temperature of course of reaction, augmenting response speed, save catalyst amount and can reach 25～30%, significantly reduce the consersion unit investment, also can reduce vapour lock simultaneously, save operating cost; (4) the present invention has dwindled the reactor apparatus volume, reduces system's floor space, makes things convenient for the installation and the maintenance of equipment.

Below Figure of description is further specified as follows: Fig. 1 is this plate-fin internal heat transfer SO ₂The structural representation of oxidation fixed bed reactors; Fig. 2 is that the A-A of Fig. 1 is to view; Fig. 3 is that continuous flat fin transverse plate wing is provided with schematic diagram; Fig. 4 is that the vertical plate wing of continuous flat fin is provided with schematic diagram; Fig. 5 is discontinuous carnassial tooth shape fin schematic diagram.

Embodiments of the present invention are comparatively simple, can adopt common sheet metal technology and machine-tooled method and equipment to process.Implement the present invention,, and be linked and packed by the described interconnected relationship of top specification and constitute flow passage structure shown in Figure 1, just can implement the present invention preferably as long as by design shown in Fig. 1～5, add each parts of cost device.For example, inventor's vertical steel plate of recommending to design by 8 thick 5mm equidistantly is separated out 4 SO that 50mm is wide in reactor ₂Cold road stream and the wide SO of 500mm ₃Hot flow path, the housing height of 3000mm, the housing width of 2200mm, 5000mm housing longitudinal length, SO ₃10 sections catalyst layers are set in the hot flow path, and the plate wing of cold-hot flow passage is all got 20 * 3mm fin, and the wing rate gets 3.

Claims

1, a kind of plate-fin internal heat transfer SO ₂The oxidation fixed bed reactors is characterized in that: it is divided into the adjacent SO of multilayer to inside reactor by polylith longitudinal metal plate ₂Raw material air cooling body runner and SO ₃Reaction gas hot body runner, reactor shell and polylith longitudinal metal plate constitute the vertical runner of equidistant parallel, and the cold fluid and hot fluid runner is alternate to be crisscross arranged SO ₃Hot flow path longitudinally is provided with multistage catalyst filling layer, in every adjacent two-stage catalytic agent packing layer heat sink wing and current limliting frame are set, corresponding cold runner side also is provided with heating plate wing, cold-hot flow passage and return header and constitutes the runner loop, be separated by between the two-stage catalytic agent packing layer is plate wing cooling surface, all be right after one section plate wing cooling surface behind every section catalyst filling layer, make in the reactor rectangular case, to constitute multichannel plate-fin internal heat transfer fixed-bed reactor; It is mainly by reactor shell (1), longitudinal metal dividing plate (2), catalyst filling layer (3), SO ₂Cold runner heating fin (4), SO ₃Hot runner cooling fin (5), catalyst filling layer frame fence (6), current limliting frame (7) and return header (8) connect and compose jointly, its interconnected relationship is: in reactor rectangular case (1), polylith longitudinal metal dividing plate (2) is arranged in parallel and constitutes SO ₂Cold runner (9) and SO ₃Hot flow path (10) is at SO ₃In the hot flow path (10), by polylith fence (6) and longitudinal metal dividing plate (2) the formation catalyst section of joining, interior loading catalyst packing layer (3), the radiating fin (5) of being gone up welding by current limliting frame (7) and longitudinal metal dividing plate (2) constitutes SO ₃The cooling duct be right after catalyst filling layer (3), at SO ₃The corresponding side surface of cooling duct constitutes SO by longitudinal metal dividing plate (2) and heating fin (4) welding ₂Heat tunnel, the top that return header (8) is placed in reactor shell (1) constitutes the cavity recirculating zone.

2, by the described a kind of plate-fin internal heat transfer SO of claim 1 ₂The oxidation fixed bed reactors is characterized in that described radiating fin (5) and heating fin (4) are vertical equity fin or horizontal vertical fins, and fin is continuous flat fin or discontinuous carnassial tooth shape fin.