Reactor for recovering reaction heat without dead angle through total reflux

Abstract

The reactor comprises a reaction section, an air inlet section, a heat exchange section, a discharging section, a liquid inlet pipe and a steam pipe, the heat exchange section is of a shell-and-tube heat exchange structure, one end of a tube pass of the heat exchange section is communicated with the air inlet section, the other end of the tube pass of the heat exchange section is communicated with the discharging section, and the liquid inlet pipe is used for supplying cold fluid to a shell pass of the heat exchange section. The steam pipe is used for releasing steam generated by a shell pass of the heat exchange section, the heat exchange section comprises a spiral flow guide mechanism, an upper pipe plate, a lower pipe plate and an array of heat exchange tube nests, the array of the heat exchange tube nests vertically penetrates through the spiral flow guide mechanism, and the upper ends and the lower ends of the heat exchange tube nests are fixed to the upper pipe plate and the lower pipe plate correspondingly; the spiral flow guide mechanism comprises a flow guide cylinder and a spiral flow guide plate, and the spiral flow guide plate is arranged in the flow guide cylinder so as to form a spiral upward shell pass.

Description

Technical Field

[0001] The utility model designs chemical reaction generating equipment, in particular to a reactor with reaction heat recovery function. Background Art

[0002] Formaldehyde is an important chemical product, and its downstream products mainly include: adhesive products for the production of urea-formaldehyde resin glue, phenol-formaldehyde resin glue and melamine-formaldehyde resin glue; polyformaldehyde, a raw material for engineering plastics with excellent comprehensive performance; polyformaldehyde, the main raw material for the production of herbicides such as glyphosate, sethoxydim, butachlor, cypermethrin, tricyclazole and other pesticides; MDI (diphenylmethane diisocyanate) is the main raw material for the production of leather PU polyurethane; anti-wrinkle agents, shrinkage-proof agents, flame retardants for clothing fabrics, etc. 35% to 40% formaldehyde aqueous solution is commonly known as formalin, which has antiseptic and bactericidal properties and can be used for soaking biological specimens, sterilization and disinfection in hospitals, etc.

[0003] More than 90% of the formaldehyde produced in industry is produced by methanol air oxidation method with methanol as raw material. Methanol air oxidation method is divided into methanol excess oxidation method (i.e. methanol silver catalytic oxidation method) and air excess oxidation method (i.e. methanol iron molybdenum catalytic oxidation method). At present, about 70% of the world's formaldehyde production capacity adopts the silver process, and about 30% adopts the iron molybdenum production process. The oxidizer is the most important key equipment in the formaldehyde production device, and it is also the most expensive of all equipment.

[0004] At present, the silver methoxide oxidation reactor uses a three-stage oxidation reactor (see Figure 1 ), that is, it consists of three parts. The upper section is the oxidation section. The ternary (or quaternary) mixed gas of methanol, air and water vapor (or tail gas) undergoes methanol oxidation reaction and releases a large amount of heat when entering the catalyst layer to generate formaldehyde gas; the middle section is a disc-ring type three-pass reaction heat recovery section heat exchanger. The high-temperature formaldehyde gas generated in the oxidation section goes through the tube side, and water goes through the shell side. The high-temperature gas is cooled. The thermal energy heats the water to generate superheated water or steam, which is separated into low-pressure steam at the top of the waste heat boiler; the lower section is the gas cooling section. The formaldehyde gas from the waste heat recovery section goes through the tube side, and the cooling water goes through the shell side. After reverse heat exchange, the formaldehyde is cooled to below 100°C.

[0005] The existing silver oxidizer reaction heat recovery section is a disc-ring type multi-pass reaction heat recovery section heat exchanger. The basic form is two upper and lower rings, and a disc in the middle, forming a center-surrounding-center three-pass circulation heat exchange. This disc-ring type heat exchanger is relatively simple to manufacture, such as Figure 1 However, this type of disc-ring tube sheet baffle heat exchanger has the following disadvantages:

[0006] 1. The water flow conditions in different places are different, the heat transfer coefficients vary greatly, and the heat exchange conditions in the entire heat exchanger are complicated.

[0007] like Figure 2 , 3 As shown: Figure 2 This is a schematic diagram of the cooling water flow path between the lower annular baffle and the lower tube plate. It can be seen from the figure that the entire disk is divided into a circulation area and a retention area; the cooling water return flow path is mainly concentrated on the four circulation pipe flow paths, that is, the circulation area. Most of the cylinder space between the four circulation pipes mainly relies on the inlet reflux to penetrate here, and then slowly floats up to the middle of the baffle ring plate under the heating of the high-temperature tube array. The cooling water here is relatively static and is the retention area.

[0008] Figure 3 This is a vertical section of the heat exchanger. It can be seen from the figure that the water flow is mainly concentrated in the large channel space between the baffles, and the retention area is mainly concentrated near the baffle tube sheet. The water flow velocity and flow form in the circulation area and the retention area are different, resulting in a large difference in the heat transfer coefficient. The heat transfer coefficient of the circulation area is large, and the heat transfer coefficient of the retention area is small. In some places, heat is even transferred by vaporization on the surface of the tubes, and the heat transfer coefficient is extremely small.

[0009] 2. The differences in heat exchange conditions lead to differences in the thermal expansion of the tubes at various locations of the rectified heat exchanger, and the heat exchange tubes "expand more and shrink less" phenomenon exists (most tubes expand more, while a few tubes expand less). This results in a large number of tubes expanding more and a small number of tubes being stretched.

[0010] Place the above Figure 2 , Figure 3 Judging from the overlapping cloud maps of the water flow direction shown in the figure, in the cooling water flow path, the heat transfer coefficient is large, the heat transfer effect is good, the temperature of the heat exchange tubes is low, and the thermal expansion is small. In the retention area, especially the plane-vertical overlap area, the water flow is small or even stationary, the heat transfer effect is poor, the temperature of the heat exchange tubes is high, and the thermal expansion is large. Huge pulling-supporting forces are generated between tubes with different expansion amounts. The tubes with large expansion amounts will be supported by the tube sheets at both ends, generating pulling forces toward both ends for the tubes with small expansion amounts. Conversely, the tubes with small expansion amounts also compress the tubes with large expansion amounts through the tube sheets at both ends, resulting in supporting forces between the tubes with large expansion amounts and the tube sheets. From Figure 2 Figure 3 It can be seen from the plane and elevation water flow cloud diagram that the number of tubes with large expansion is far greater than the number of tubes with small expansion, and the two are about 2 to 3 times, which causes the tensile tubes to be at a disadvantage.

[0011] 3. In some areas near the baffles, due to the large temperature difference between the inside and outside of the parallel tubes due to the poor water flow, the cooling water vaporizes and bursts rapidly, causing cavitation on the surface of the heat exchange tubes. During the heat exchange process, relatively static water will occur when the temperature difference is 200 to 300 degrees: the water on the surface does not have time to transfer heat, causing the water on the surface of the heating block to vaporize rapidly, and the superheated bubbles generated will burst instantly when they encounter the water on the outside. This rapid vaporization and instantaneous bursting on the surface of the heat exchange tubes is like countless "micro-explosions", causing the entire water body to vibrate, which will cause damage to nearby solids, namely cavitation. From the vertical water flow cloud map, it can be seen that this damage is mainly concentrated on both sides of the ring-disc baffles, and the upper side of the baffles is more serious. At the top of the heat exchanger, there is a temperature difference of more than 500 degrees between the 600-700℃ high-temperature product that has just reacted and the cooling water of about 130-150℃ on the outside of the tube, resulting in more serious cavitation on the upper side of the upper baffle tube plate. Cavitation causes the surface of the heat exchange tubes to be damaged and the strength to be reduced.

[0012] In summary, the complex flow conditions lead to asynchronous thermal expansion of tubes at different locations, and the number of tubes with small thermal expansion is at a disadvantage and in a tensile state, resulting in cavitation on the surface of the heat exchange tubes near the baffle surface. This ultimately leads to the destructive event of "the heat exchange tubes in certain areas are concentrated and neatly broken". Utility Model Content

[0013] The utility model aims at the drawbacks of the above-mentioned prior art reaction heat exchanger, and provides a reactor with full reflux and no dead angle to recover reaction heat, which is applied to silver method methanol oxidation to formaldehyde.

[0014] The technical solution adopted by the utility model to solve the above-mentioned problem is: a reactor, comprising: a reaction section, an air inlet section, a heat exchange section, a discharge section, a liquid inlet pipe and a steam pipe, the heat exchange section is a shell and tube heat exchange structure, one end of the tube side of the heat exchange section is connected to the air inlet section, and the other end is connected to the discharge section, the liquid inlet pipe is used to supply cooling fluid to the shell side of the heat exchange section, and the steam pipe is used to release the steam generated in the shell side of the heat exchange section, characterized in that: the heat exchange section comprises: a spiral guide mechanism, an upper tube plate, a lower tube plate, and an array of heat exchange tubes, the array of heat exchange tubes passes through the spiral guide structure from top to bottom, the upper and lower ends of the heat exchange tubes are respectively fixed on the upper tube plate and the lower tube plate, the spiral guide mechanism comprises a guide tube and a spiral guide plate, and the spiral guide plate is arranged inside the guide tube to form a spiral shell side.

[0015] As one of the preferred embodiments of the present application, the reactor further comprises an equipment barrel, the heat exchange section is located inside the equipment barrel, an annular channel is formed between the flow guide barrel and the equipment barrel, and the spiral flow guide mechanism is connected to the annular channel at the bottom.

[0016] As one of the preferred embodiments of the present application, the center of the guide tube is a central mixed flow area that runs through from top to bottom, and the spiral guide plate surrounds the central mixed flow area. The fluid spiraling up along the spiral guide plate converges to the central mixed flow area while surging upward, thereby improving the heat exchange efficiency of the central heat exchange tube and helping to achieve uniform heat exchange inside the guide tube.

[0017] As one of the preferred embodiments of the present application, the spiral flow guide mechanism further includes a cold and hot flow diverter plate, which is arranged at the upper end of the flow guide cylinder, and the annular channel extends upward to the outside of the cold and hot flow diverter plate, so as to achieve uniform inflow of cold fluid into the bottom of the central flow guide cylinder.

[0018] As one of the preferred embodiments of the present application, the angle α between the outer spiral surface of the spiral guide plate and the horizontal plane is 15 to 70°, preferably 20 to 50°.

[0019] As one of the preferred embodiments of the present application, there are multiple spiral guide plates, which are evenly arranged in the guide tube relative to the central axis of the guide tube. The number of spiral guide plates is preferably an integer multiple of 6 to form multiple spiral flow channels.

[0020] As one of the preferred embodiments of the present application, a cold fluid guide plate is provided at the bottom of the annular channel, and the cold fluid guide plate is evenly distributed along the annular direction of the spiral guide mechanism for evenly guiding the annular channel to the spiral guide mechanism, which helps to achieve even liquid inflow to the spiral guide mechanism.

[0021] As one of the preferred embodiments of the present application, the cold fluid guide plate is arranged on the lower tube plate, and the angle β between the cold fluid guide plate and the horizontal radial direction of the lower tube plate is 0 to 60°, so as to realize the spiral uniform liquid inflow into the spiral guide mechanism.

[0022] As one of the preferred embodiments of the present application, the upper end of the guide tube is concentrically provided with a flow tube upper fixing ring, an upper outer ring, and an upper inner ring, and the three are connected as a whole and fixed to the guide tube through an upper radial support; the lower end of the guide tube is concentrically provided with a flow tube lower fixing ring, a lower outer ring, and a lower inner ring, and the three are connected as a whole and fixed to the guide tube through a lower radial support, and a fixing rod is passed through between the upper outer ring and the lower outer ring, and between the upper inner ring and the upper inner ring, and the ends of the fixing rod are connected to the upper tube sheet and the lower tube sheet. This support structure is helpful for the structural installation of the spiral guide plate and improves the structural strength.

[0023] Compared with the prior art, the reactor of the present application has the following advantages:

[0024] 1. The cooling water keeps flowing at all points inside and outside the heat exchanger, and there are no dead corners such as stagnation areas.

[0025] 2. The high-temperature medium in the heat exchanger flows from top to bottom, and the cooling water flows from bottom to top, which is a complete countercurrent heat exchange, and the heat exchange form is the best.

[0026] 3. The cooling water fluid in the heat exchanger flows in a spiral plunger shape, and the fluid flushes the tube bundle horizontally for cross-flow heat exchange, maintaining the heat transfer coefficient of the heat exchange tubes at the optimal level.

[0027] 4. After the cooling water is heated, its specific gravity decreases and it floats up. During the floating process, the water flow has the characteristic of diverting and compensating to the part with large lifting curvature. The cooling water naturally compensates to the center of the cooler, maintaining the normal distribution of the maximum flow in the center, ensuring sufficient cooling water flow under the high-temperature upper tube plate, and avoiding the rapid vaporization phenomenon caused by the large temperature difference under the upper tube plate due to the high flow rate. Rapid vaporization will cause vibration of the entire reactor.

[0028] 5. The cooling water flow channel is smooth and consistent, the cooling water flows in the same direction, and there is no "collision" flow direction; the flow cross-sections have the same area and shape, and there is no sudden change in the flow cross-section, flow velocity and direction; the flow cross-section is maximized and the system flow resistance is minimized.

[0029] 6. The cooling water in the heat exchanger flows smoothly, and there is no local violent vaporization-burst, which causes cavitation on the surface of the heat exchange tubes and reduces the strength.

[0030] 7. The system runs smoothly and stably without vibration, and there is no need to thicken the spiral guide plate to improve the structural strength.

[0031] 8. The spiral guide mechanism has a simple structure, uses less material, has low structural strength requirements, and is easy to process. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 It is a structural schematic diagram of an existing silver methoxide oxidation reactor;

[0033] Figure 2 A top view of the cold water circulation mode of the reaction heat recovery section of the existing reactor;

[0034] Figure 3 It is the distribution diagram of the retention area and circulation area of ​​the reaction heat recovery section of the existing reactor;

[0035] Figure 1-3 Among them, 1, reactant outlet 2, lower head 3, lower tube sheet 4, heat exchange tube 5, lower annular baffle 6, equipment barrel 7, middle disc baffle 8, upper annular baffle 9, cooling water circulation pipe 10, gas-liquid separation partition 11, upper tube sheet 12, air inlet section 13, sight glass 14, equipment large flange 15, raw gas inlet 16, gas distributor 17, upper head 18, by-product steam outlet 19, water supply port A, flow area B, retention area.

[0036] Figure 4 This is a schematic diagram of the structure of a reactor for producing formaldehyde by oxidation of methanol using a silver method according to an embodiment of the present invention;

[0037] Figure 5 The fluid flow mode corresponding to the heat exchange section of the reactor in the embodiment of the present invention;

[0038] Figure 6 A top view of the circulation mode of the cold and hot fluids in the heat exchange section of the reactor in an embodiment of the present invention;

[0039] Figure 7 It is a schematic diagram of the arrangement structure of the cold fluid guide plate relative to the lower tube plate in an embodiment of the present invention;

[0040] Figure 8 Schematic diagram of the structure of the spiral flow guide mechanism in an embodiment of the present invention;

[0041] Fig. 9 Another structural schematic diagram of the spiral flow guide mechanism in an embodiment of the present invention;

[0042] Fig.10 It is a schematic diagram of the structure of the spiral flow guide mechanism in the embodiment of the present invention without the cold and hot flow splitter plate and the cold fluid flow guide plate;

[0043] Figure 4-10 Among them, 1, reactant outlet 2, lower head 3, lower tube sheet 4 heat exchange tube 5, spiral guide mechanism 6, equipment barrel 7, upper tube sheet 8, air inlet section 9, water inlet pipe 10, sight glass 11, equipment large flange 12, raw gas inlet 13, gas distributor 14, upper head 15, by-product steam outlet 52, guide tube 53, spiral guide plate 55, guide mechanism fixing rod 56, cold and hot flow diverter plate 57, cold fluid guide plate 511, guide tube lower fixing ring 512, lower outer ring 513, lower radial support 514, lower inner ring 541, guide tube upper fixing ring 542, upper outer ring 543, upper radial support 544, upper inner ring. DETAILED DESCRIPTION

[0044] The present invention is further described in detail below in conjunction with the accompanying drawings. The embodiments are exemplary and intended to be used to explain the present invention, but should not be understood as limiting the present invention. The text description in this embodiment corresponds to the accompanying drawings, and the description of the orientation is also based on the description of the accompanying drawings, and should not be understood as limiting the scope of protection of the present invention.

[0045] like Figure 4-10As shown, in the reactor for recovering reaction heat with full reflux without dead angle in this embodiment, the spiral guide mechanism 5 is used as a heat exchange section for recovering reaction heat below the air inlet section 8. The reaction atmosphere enters the heat exchange tubes 4 through the air inlet section 8, i.e., it goes through the tube side; the cooling medium is usually water and goes through the shell side of the guide tube 52. The reaction atmosphere is from top to bottom, and the cooling medium is from bottom to top, and countercurrent heat is exchanged in the spiral guide mechanism. The spiral guide mechanism 5 is located inside the equipment barrel 6, and a ring channel with uniform width is formed between the guide tube 52 and the equipment barrel 6. The water inlet pipe 9 passes through the equipment barrel 6 and extends to the ring channel, which is used to supplement the cold fluid to the ring channel. The cold fluid flows downward through the ring channel and then diffuses into the inside of the guide tube 52.

[0046] The lower fixing ring 511, the lower outer ring 512, the lower radial support 513, and the lower inner ring 514 of the guide tube constitute the lower fixing structure of the spiral guide plate 53 on the guide tube 52, and the upper fixing ring 541, the upper outer ring 542, the upper radial support 543, and the upper inner ring 544 of the guide tube constitute the upper fixing structure of the spiral guide plate 53 on the guide tube 52, and then the guide mechanism fixing rod 55 is used to fix the entire spiral guide mechanism 5 on the upper tube plate 7 by threaded connection. The upper end of the spiral guide plate 53 is fixed to the upper outer ring 542 and the upper inner ring 544 by welding, riveting, fixing bolts or clamping, etc.; the lower end is fixed to the lower outer ring 512 and the lower inner ring 514 by welding, riveting, fixing bolts or clamping, etc. The guide tube 52 is fixed to the upper and lower guide tube fixing rings 511 and 541 by welding, riveting, fixing bolts or clamping, etc.

[0047] As an optional structure, the hot and cold flow splitter plate 56 is added to the fixing ring 541 on the guide tube by welding, riveting, fixing bolts or clamping.

[0048] As an optional structure, a circle of cold fluid guide plates 57 is welded on the lower tube sheet 2 below the guide mechanism 5 to further optimize the cooling water flow state of the heat exchange section. The circle of cold fluid guide plates 57 welded on the lower tube sheet 2 has a horizontal radial angle β between 0 and 60° with the equipment tube sheet. The guide plate angle is set according to specific working conditions. The guide plate not only has a guiding function, but also further strengthens the structure of the lower tube sheet 2.

[0049] The spiral guide plate 53 in this embodiment is a continuous smooth guide plate, and axial openings are provided at corresponding positions of the guide mechanism fixing rod 531 and the heat exchange tube array 4.

[0050] The angle α between the outer spiral surface of the spiral guide plate 53 and the horizontal plane is between 15° and 70°, preferably between 20° and 50°.

[0051] As an optional structure, the arrangement of the heat exchange tubes 4 is selected to be arranged in an equilateral triangle arrangement at the center point, and diffused to the surrounding of the tube sheet in a regular hexagonal route to cover the entire tube sheet. The number of spiral guide plates 53 is selected to be an integer multiple of 6, which is convenient for spiral plate molding and punching (one-time molding, one-time punching).

[0052] The heat exchange section of the silver-based methanol oxidation reactor for formaldehyde production without dead angle full reflux heat exchange, the cooling water flow state is as follows Figure 5-6 shown.

[0053] The cooling soft water is injected into the cold fluid layer in the gas-liquid separation section, and flows down along the annular channel between the equipment cylinder 6 and the guide tube 52. It flows from all sides to the central heat exchange tube array 4 array under the guide mechanism 5. The water is heated in the heat exchange tube array. The specific gravity is reduced, and the water flows upward. The difference in specific gravity inside and outside the spiral guide mechanism 5 generates a driving force. Under the pressure difference between the inside and outside, the water flows in an overall spiral along the direction of the spiral guide plate. The water flows horizontally through the heat exchange tube array and exchanges heat with the high-temperature gas in the tube. The cooling water is heated into a hot fluid, overflows the hot and cold flow diverter plate at the top of the spiral guide mechanism 5, and enters the gas-liquid separation section. The hot fluid flashes to produce steam cold, but it cools down and becomes a cold fluid that sinks. At the same time, it is mixed with the fresh cooling water that enters and flows down along the annular channel between the equipment cylinder 6 and the guide tube 52, and the cycle repeats.

[0054] It has the following features:

[0055] 1. The cooling water inlet and outlet of the spiral circulation cooler are completely open, and the cold fluid annular channel outside the spiral guide mechanism is uniform.

[0056] 2. The spiral guide plate is lifted axially with a continuous and smooth transition. All guide plates are processed in the same mold to keep the cross-section of all flow channels of the heat exchanger mechanism consistent.

[0057] 3. Each vertical cross-sectional line of the spiral guide plate remains horizontal, and the curvature (lifting angle) of the spiral surface of the spiral guide plate increases smoothly from the outside to the inside.

[0058] Practice shows that spiral heat exchangers have the following advantages compared to baffle heat exchangers:

[0059] (1) When the mass flow rate is the same, the pressure drop of the continuous spiral baffle heat exchanger is about 1 / 2 to 1 / 4 times that of the existing heat exchanger; and the greater the flow rate, the greater the pressure drop difference between the two.

[0060] (2) The heat transfer coefficient of the continuous spiral baffle heat exchanger remains balanced and stable, and the total heat transfer coefficient is increased by 30% to 50% compared with the existing heat exchanger, which is about 1.3 to 1.5 times that of the existing heat exchanger.

[0061] (3) Under the same working conditions, the temperature of the cooling water hot fluid of the continuous spiral baffle heat exchanger is 5 to 10°C lower than that of the existing oxidizer heat exchanger, and the reactant composition is better than that of the existing oxidizer.

[0062] Structure: 1

[0063] 20kt / a oxidizer waste heat recovery section: guide tube 52 height H = 1350mm, diameter φ1200mm, cylinder 6 diameter φ1400mm; spiral guide plate 53, 6 pieces in total, evenly distributed in the circumference, plate width 500mm, plate thickness 0.5mm, material SUS304, spiral angle α25°; cold fluid guide plate 57, 44 pieces in total, evenly distributed in the circumference, plate height 300mm, radial angle β30° with lower tube plate 3

[0064] Structure: 2

[0065] 60kt / a oxidizer waste heat recovery section: guide tube 52 height H = 1200mm, diameter φ2000mm, cylinder 6 diameter φ2200mm; spiral guide plate 53 has 12 pieces evenly distributed in the circumference, plate width 800mm, plate thickness 2mm, material Q235B, spiral angle α30°; cold fluid guide plate 57 has 69 pieces evenly distributed in the circumference, plate height 450mm, radial angle β5° with lower tube plate 3

[0066] In addition to the above embodiments, the present invention also includes other implementation modes. Any technical solutions formed by equivalent transformation or equivalent replacement should fall within the protection scope of the claims of the present invention.

Claims

1. A reactor comprising: A reaction section, an air inlet section, a heat exchange section, a discharge section, a liquid inlet pipe and a steam pipe, wherein the heat exchange section is a shell and tube heat exchange structure, one end of the tube side of the heat exchange section is connected to the air inlet section, and the other end is connected to the discharge section, the liquid inlet pipe is used to supply cooling fluid to the shell side of the heat exchange section, and the steam pipe is used to release the steam generated in the shell side of the heat exchange section, characterized in that: the heat exchange section comprises: a spiral guide mechanism, an upper tube plate, a lower tube plate, and an array of heat exchange tubes, the array of heat exchange tubes passes through the spiral guide structure from top to bottom, and the upper and lower ends of the heat exchange tubes are respectively fixed on the upper tube plate and the lower tube plate, the spiral guide mechanism comprises a guide tube and a spiral guide plate, and the spiral guide plate is arranged inside the guide tube to form a spiral shell side.

2. The reactor according to claim 1, characterized in that: It also includes an equipment cylinder, the heat exchange section is located inside the equipment cylinder, an annular channel is formed between the guide cylinder and the equipment cylinder, and the spiral guide mechanism is connected to the annular channel at the bottom.

3. The reactor according to claim 1, characterized in that: The center of the guide tube is a central mixed flow area that runs through from top to bottom, and the spiral guide plate surrounds the central mixed flow area.

4. The reactor according to claim 2, characterized in that: The spiral flow guide mechanism also includes a cold and hot flow diverter plate, which is arranged at the upper end of the flow guide cylinder, and the annular channel extends upward to the outside of the cold and hot flow diverter plate.

5. The reactor according to claim 1, characterized in that: The included angle α between the outer spiral surface of the spiral guide plate and the horizontal plane is 15 to 70 degrees.

6. The reactor according to claim 5, characterized in that: The included angle α between the outer spiral surface of the spiral guide plate and the horizontal plane is 20 to 50°.

7. The reactor according to claim 1, characterized in that: There are a plurality of spiral guide plates, which are evenly arranged in the guide tube relative to the central axis of the guide tube.

8. The reactor according to claim 2, characterized in that: A cold fluid guide plate is arranged at the bottom of the annular channel, and the cold fluid guide plate is evenly distributed along the annular direction of the spiral guide mechanism for evenly guiding the annular channel to the spiral guide mechanism.

9. The reactor according to claim 8, characterized in that: The cold fluid guide plate is arranged on the lower tube plate, and the angle β between the cold fluid guide plate and the lower tube plate in the horizontal radial direction is in the range of 0 to 60°.

10. The reactor according to claim 1, characterized in that: An upper fixing ring, an upper outer ring and an upper inner ring are concentrically arranged at the upper end of the guide tube, and the three are connected as a whole and fixed to the guide tube via an upper radial support; a lower fixing ring, a lower outer ring and a lower inner ring are concentrically arranged at the lower end of the guide tube, and the three are connected as a whole and fixed to the guide tube via a lower radial support, a fixing rod passes through the upper outer ring and the lower outer ring, and between the upper inner ring and the upper inner ring, and the end of the fixing rod is connected to the upper tube plate.

Images