A reactor with optimized temperature and its reaction process and application

Abstract

The present invention discloses a reactor with a simple and reliable structure and high synthesis efficiency. The reactor comprises a shell, a heat exchange internal part composed of heat exchange tubes, and a catalyst basket with a porous gas distribution plate. The center of the catalyst basket is provided with a porous gas collecting pipe or a porous gas distribution pipe. The shell is provided with an air inlet and an air outlet for reaction gas, a catalyst loading and unloading port, a manhole, a water inlet pipe box and a water outlet steam pipe box for a heat exchange tube bundle. The inner basket of the catalyst basket is provided with a heat exchange zone composed of multiple rows of heat exchange tubes. There is an insulation zone without heat exchange tubes between the inner and outer heat exchange zones. The two ends of the heat exchange tubes of multiple concentric ring heat exchange zones are respectively connected to the water inlet pipe box and the water outlet steam pipe box. The present invention also discloses a production process using the reactor with significant energy saving and consumption reduction.

Description

Technical Field

[0001] The invention relates to the field of chemical engineering, and in particular to a temperature-optimized reactor and an applicable reaction process thereof. Background Art

[0002] For exothermic catalytic reactions such as ammonia synthesis under pressure, as the reaction process proceeds, the reaction heat continuously released causes the catalyst layer temperature to increase. In order to improve the efficiency of the reactor, the reaction heat needs to be removed to maintain the most suitable reaction temperature. The inventor has invented a catalytic reaction device close to the optimal reaction temperature, and obtained Chinese invention patent CN96111851.2 and US invention patent US6214296, which was used in an ammonia synthesis tower and successfully put into operation, achieving good results. However, this technology recovers the reaction heat and by-product medium and low-pressure steam outside the synthesis tower. Now ammonia synthesis is developing in the direction of recovering high-pressure by-product steam and saving energy and reducing consumption. For example, the three-tower three-waste boiler process of Brown Company abroad, and the double-tower and double-waste boiler of Topsoe and Wood Company are both by-product steam outside the synthesis tower.

[0003] Up to now, large-scale ammonia synthesis units that have been industrialized at home and abroad are composed of ammonia synthesis and reaction heat recovery and cooling and separation of product ammonia from synthesis gas. Figure 1 This is the flow chart of the ammonia synthesis circle of the foreign Brown Company. As can be seen from the figure, this Brown ammonia synthesis unit with a daily output of 1,000 tons consists of three ammonia synthesis towers connected in series. The outlet of each synthesis tower is connected to a waste heat boiler to recover the reaction heat and produce high-pressure steam to reduce the temperature of the synthesis gas before entering the next ammonia synthesis tower. That is, the ammonia synthesis reaction and the reaction heat recovery are carried out separately in two independent equipment, and then the reaction gas is cooled to a low temperature of 4.4℃ by a water cooler and ammonia cooling air to further separate the liquid ammonia. After the ammonia separation, a small part of the gas is discharged as purge gas, and most of the circulating machine is combined with the synthetic raw gas and the pressure is increased by the circulating machine to return to the ammonia tower for further synthesis of ammonia.

[0004] KBR's isothermal ammonia reactor (EP0994072) patent proposed that a shell-and-tube reactor be used in an ammonia synthesis loop, with catalysts installed in the tubes. The raw gas enters from the upper air inlet and is distributed in each tube, synthesized in the catalyst layer in the tubes, and water enters the sides between the tubes. The reaction heat is continuously transferred by boiling water outside the tubes, and the generated steam is discharged from the side tubes, and the reaction gas is discharged from the bottom outlet pipe. The tower has a small temperature difference and uses a high-priced precious metal ruthenium-based ammonia synthesis catalyst. It is suitable for operation at low temperatures of 315 to 435°C, and is not suitable for the high-temperature use temperature of a large number of iron-based catalysts. In addition, the shell-and-tube reactor has a small catalyst filling coefficient, low volume utilization, and unreliable reaction tube fixing and welding structures. The investment is high and it is difficult to scale up.

[0005] The above-mentioned foreign methods all have the disadvantages of long process flow, many required equipments and large investment. Summary of the invention

[0006] In order to overcome the above-mentioned deficiencies of the prior art, the present invention provides a reactor with a simple and reliable structure and high synthesis efficiency, as well as a production process using the reactor with significant energy saving and consumption reduction.

[0007] A temperature-optimizing reactor, the reactor comprising a shell, heat exchange internals consisting of heat exchange tubes, and a catalyst basket with a porous gas distribution plate, the center of the catalyst basket is provided with a porous gas collecting pipe or a porous gas distribution pipe, the shell is provided with an air inlet and an air outlet for reaction gas, a catalyst loading and unloading port, a manhole, a water inlet pipe box and a water outlet steam pipe box for a heat exchange tube bundle, the inner basket of the catalyst basket is provided with a heat exchange zone consisting of a plurality of rows of heat exchange tubes distributed according to the cross section, an insulating zone without heat exchange tubes is provided between the inner and outer heat exchange zones, the heat exchange zone and the insulating zone are spaced by a porous annular sleeve and arranged at intervals according to concentric annular rings, the two ends of the heat exchange tubes of the plurality of concentric annular heat exchange zones are respectively connected to the water inlet pipe box and the water outlet steam pipe box, the water inlet pipe box and the water outlet steam pipe box are connected in series with a single steam drum with a steam pressure regulating pipeline directly or through a circulating water pump to form a circulation loop, and the temperature of each layer of each heat exchange zone and the insulating zone is independently adjusted by adjusting the vaporization pressure of the heat exchange medium to adjust the vaporization temperature. When there are multiple circulation loops, each circulation loop may contain a different heat exchange medium.

[0008] When the above reactor is in use, the raw reaction gas enters the reactor through the air inlet on the shell, enters the middle of the outer shell and the catalyst basket, and flows centripetally through the porous distributor through the catalyst layers in the adiabatic zone and the heat exchange zone to the porous gas collecting pipe, or conversely, enters from the bottom air inlet, passes through the central porous gas distribution pipe from the inside to the outside centrifugally through the catalyst layers in the adiabatic zone and the heat exchange zone layer by layer for reaction, passes through the shell to the upper part, and exits the tower through the top air outlet for reaction gas. The circulation loop connecting the inner heat exchange zone and the steam drum and the circulation loop connecting the outer heat exchange zone and the steam drum can independently adjust the heat exchange inside and outside of the reactor and the reaction of the adiabatic catalyst by adjusting the pressure regulating valve on the steam drum respectively.

[0009] The inside and outside of the catalyst basket and one side of the catalyst outside the central gas distribution or gas collection pipe are all provided with wire meshes.

[0010] The heat exchange tubes in the heat exchange zone are spirally wound tubes.

[0011] For high-pressure synthesis reactors such as those used for ammonia synthesis that require pressures of more than 10MPa, in order to reduce the material requirements and usage for the high-pressure shell, a centripetal radial reactor can be selected. At this time, the main line of the reaction gas enters from the top of the reactor, and a cold secondary line inlet hole is set at the bottom of the reactor. Part of the low-temperature gas flows upward from the bottom to the top through the outer shell wall and the catalyst basket to reduce the temperature of the outer shell tower wall, and is evenly mixed in the space above the top catalyst. Because the top of the reactor center tube is sealed and about 5% of the tube length has no holes in the tube wall, a small amount of gas reacts axially from top to bottom through the catalyst layer, and most of the mixed raw gas flows from top to bottom with the inner wall of the catalyst basket and the gas distribution chamber of the cylindrical porous gas distribution plate, and evenly passes through the gas distribution plate and the porous wire mesh from the outside to the inside to the adiabatic and heat exchange catalytic reaction zone to the porous central gas collecting cylinder, and the reaction gas exits the reactor from top to bottom from the bottom.

[0012] A process method using the reactor as described above, wherein the synthesis gas is heated by a heat exchanger and then enters the reactor for reaction, the reactor is externally connected to a circulation loop including a steam drum, the high temperature generated by the reaction gas during the reaction heats the heat exchange medium to generate steam, the gas after the reaction exits the reactor and exchanges heat with the synthesis gas before entering the tower, and then passes through an air cooler and a water cooler or a water cooler and an ammonia cooler, and then is separated into gas and liquid in a gas-liquid separator.

[0013] The process method is used for an ammonia synthesis device, and adopts low-pressure and isobaric ammonia synthesis technology for preparing synthesis gas from coal or residual oil, and the ammonia synthesis pressure is ≤22MPa, preferably ≤18MPa.

[0014] The process is used in an ammonia synthesis device, using an iron, ferrous or iron-cobalt or ruthenium-based ammonia synthesis catalyst, with a maximum catalytic temperature of less than 480°C.

[0015] The circulation ratio of the ammonia synthesis circulating gas volume to the raw material gas volume is less than 2.5, and the synthesis purge gas is used to recover effective hydrogen by membrane separation and other methods.

[0016] The process method for producing methane from synthesis gas adopts isobaric methanation with the same pressure as the raw synthesis gas or high-pressure methanation of >5MPa.

[0017] The reactor is used for high-temperature fixed-bed gas-solid phase catalytic reaction of methanol dehydration to produce olefins and gasoline, namely MTP, MTO, MTG, at a reaction temperature of more than 300°C, and o-xylene oxidation to produce phthalic anhydride.

[0018] Compared with other existing reactors, the reactor of the present invention has many outstanding advantages:

[0019] 1. Reaction and steam production are integrated, temperature control and steam production are integrated, and the structure is simple and reliable.

[0020] 2. The reactor components have no thermal stress, and the heat exchange tubes have no welding points in the reaction area, ensuring the intrinsic safety of the reactor.

[0021] 3. Radial tower, fine-grained small catalyst, small diffusion resistance within the catalyst, high activity and high synthesis efficiency.

[0022] 4. The heat transfer efficiency is high, the catalyst layer is in the optimal reaction temperature zone, the temperature difference is small, the temperature adjustment by steam pressure is convenient and stable, the temperature adjustment is carried out in layers, and the catalyst life is long.

[0023] 5. The catalyst is installed outside the heat exchange tube, which has a filling factor more than 2 times higher than that of the shell-and-tube ammonia synthesis tower with the catalyst installed inside the heat exchange tube, and the reactor size and investment are greatly reduced.

[0024] 6. The synthesis loop process is short, the equipment is small, the investment is greatly reduced, the resistance is small, the energy consumption is low, the energy saving and consumption reduction are significant, and the production cost per ton of product is reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 This is the flow chart of the ammonia synthesis cycle of the foreign Brown Company.

[0026] Figure 2 It is a schematic structural diagram of the reactor of the present invention.

[0027] Figure 3 It is a schematic diagram of the transverse cross-sectional structure of the reactor of the present invention, in which one layer of heat exchange area and two layers of insulation area are provided.

[0028] Figure 4 This is another schematic diagram of the transverse cross-sectional structure of the reactor of the present invention, in which two layers of heat exchange areas and three layers of insulation areas are provided.

[0029] Figure 5 Flow chart of the process of the present invention.

[0030] Description of reference numerals:

[0031] 1- Shell 2- Heat exchange tube 3- Porous gas distribution plate 4- Air inlet

[0032] 5-air outlet 6a-catalyst loading port 6b-catalyst unloading port 7-water inlet box

[0033] 8- outlet steam pipe box 9- steam drum 10- water pump 11a- outer wire mesh

[0034] 11b-inner screen 12-central tube 13-separation tube 14-catalyst

[0035] 15-cold secondary line air inlet 16-support rod I-heat exchange area II-insulation area

[0036] R-synthesis tower E1-heat exchanger E2-water cooler E3-cold exchange

[0037] E4- Ammonia Cooler E5- Start-up Heater C- Circulator S- Ammonia Separator DETAILED DESCRIPTION

[0038] Example 1

[0039] like Figure 2 The reactor of the present invention shown in the figure comprises a shell 1, a heat exchange internal part composed of a heat exchange tube 2, and a catalyst basket with a porous gas distribution plate 3. The center of the catalyst basket is provided with a central tube 12 as a porous gas collecting pipe, and the central tube 12 is fixed in the reactor by a support rod 16. The shell 1 is provided with a reaction gas inlet 4 and a gas outlet 5, a catalyst loading port 6a (also serving as a manhole), a catalyst unloading port 6b (also serving as a manhole), a water inlet pipe box 7 and a water outlet pipe box 8 connecting the two ends of the heat exchange tube 2. The inner basket of the catalyst basket is provided with a heat exchange zone I (see FIG. 1 ) where the heat exchange internal part is located according to the cross section. Figure 3 ), there is an insulation zone II without heat exchange internals between the inner and outer heat exchange zones (see Figure 3 ), the heat exchange zone I and the insulation zone II are arranged in concentric circles, the heat exchange internals are composed of multiple groups of heat exchange tubes arranged in clockwise and counterclockwise directions, and the two ends of the heat exchange tubes in the heat exchange zone I are respectively connected to the water inlet pipe box 7 and the water vapor outlet pipe box 8. The transverse section of the reactor is as follows Figure 3 As shown, a wire mesh 11 is provided on the inner wall of the gas distribution plate in the catalyst basket and on one side of the catalyst outside the central gas collecting pipe.

[0040] The process diagram using the above reactor is as follows Figure 5 As shown, the reactor, i.e., the synthesis tower R, is provided with a drum 9 and a water pump 10 with a circulation loop externally connected to a pressure regulating valve steam outlet pipe and a water supply pipe. The synthesis tower R is connected to a heat exchanger E1, a water cooler E2, an ammonia separator S, a cold exchanger E3, and an ammonia cooler E4. The circulation machine C is connected to the heat exchanger E1. The synthesis gas is heated by the heat exchanger E1 and enters the synthesis tower R for reaction. The high temperature generated by the reaction gas during the reaction heats the heat exchange medium to generate steam. The gas after the reaction exits the synthesis tower R and exchanges heat with the synthesis gas before entering the tower, and then cools down by the water cooler E2, enters the ammonia separator S to separate liquid ammonia, and then passes through the cold exchanger E3 and the ammonia cooler E4. A small part is used as purge gas, and the other most part enters the circulation machine C to mix with the synthesis gas. A start-up heater E5 is also provided on the inlet pipeline of the synthesis tower R for heating the ammonia synthesis catalyst and reducing the catalyst during startup.

[0041] Most of the raw reaction gas is heated to 350°C through heat exchange and enters the reactor through the air inlet 4 on the top of the shell 1. In addition, part of the low-temperature synthesis gas from the circulation machine C that has not been heated by the heat exchanger enters through the cold bypass air inlet 15 at the bottom of the reactor R, and reaches the upper space of the reactor from bottom to top along the channel between the shell 1 and the catalyst basket close to the side of the shell 1, mixes with the reaction gas coming in from the air inlet 4, and then flows from top to bottom through the channel between the shell 1 and the catalyst basket close to the side of the catalyst basket, through the porous gas distribution plate 3, and centripetally flows through the catalyst layers of the insulation zone II and the heat exchange zone I one by one to the central tube 12 used as a porous gas collecting pipe, and then flows downward in the central tube 12 to exit the reactor from the air outlet 5.

[0042] Example 2

[0043] Ammonia synthesis reactor with a daily output of 1,000 tons, with a structure like Figure 3 As shown, a heat exchange zone I is provided inside, and an insulation zone II is provided inside and outside the heat exchange zone I. The heat exchange coil connects the lower water inlet pipe box 7 and the upper water vapor outlet pipe box 8. The catalyst basket is filled with 80M small particles of high-activity domestic ammonia synthesis catalyst (CN01135660) with a diameter of 1.5 to 3 mm. 3 The two ends of the heat exchange tube are connected to the water inlet pipe box 7 and the water outlet steam pipe box 8 respectively, and are connected in series with a single steam drum 9 with a steam pressure regulating pipeline and a circulating water pump 10 to form a circulation loop. Figure 4 As shown, the temperature of each layer in the heat exchange zone and the insulation zone can be independently adjusted by adjusting the vaporization pressure of the heat exchange medium and adjusting the vaporization temperature.

[0044] The main indicators of the synthesis circle of this embodiment and the indicators of the foreign Brown and Topsoe company (see Li Qiongjiu, ed., Synthetic Ammonia and Carbon One Chemistry, Sichuan Science and Technology Press, page 495) are shown in the second column "Example 1", the second column "Brown" and the third column "TopsΦe" of Table 1.

[0045] Table 1

[0046]

[0047] Example 3

[0048] Use Figure 2 The reactor structure shown in the figure is different from that of Example 2 in that the reactor of this embodiment is provided with two inner and outer annular heat exchange zones and three insulation zones (see Figure 4 ), the heat exchange zone and the adiabatic zone are arranged at intervals, and the heat exchange pipes of the two heat exchange zones respectively form a water circulation loop with the water inlet pipe box and the water outlet steam pipe box, the steam drum and the circulating water pump. The circulation loop connecting the inner heat exchange zone and the steam drum and the circulation loop connecting the outer heat exchange zone and the steam drum can independently adjust the reaction of the catalyst in the heat exchange zone and the adiabatic zone of the reactor by adjusting the pressure regulating valve on the steam drum. The catalyst basket is filled with domestic high-activity catalyst 79M 3(particle size 1.5-3 mm), catalyst layer inlet temperature 350° C., hot spot temperature 415° C., outlet temperature 400° C. For specific data, see Table 1, column 5, “Example 2”.

[0049] Example 4

[0050] The reactor structure of the present application is used for methane synthesis, with three layers of coiled heat exchange zones, and insulation zones between the heat exchange zones (four in total). The heat exchange coils form a three-way water vapor circulation system through upper and lower pipe boxes and three independent steam drums, and are equipped with domestically produced Dalian Institute of Chemical Physics nickel-based high-activity methanogenic catalyst 76M 3 Each circuit consists of two inlet and outlet water tanks arranged symmetrically at 180 degrees from top to bottom.

[0051] The main indicators of the methanogenization technology of this embodiment and the foreign DAVY company are compared in Table 2 (see "Natural Gas Chemical Industry" 2013 Issue 6 Page 4245)

[0052] Table 2 Main indicators of this embodiment and foreign methanogenation reactors

[0053]

[0054] Example 5

[0055] Methanol dehydration to olefins. Ningxia, China, produces 1.67 million tons of methanol to produce 500,000 tons of olefins (MTP) annually. In 2006, it signed a technology licensing fee of 130 million yuan with a foreign company. There are three MTP reactors, two of which are in operation and one is on standby (Coal Chemical Handbook, edited by Xu Zhengang, Chemical Industry Press). The structure of the MTP reactor can be found in PCT patent WO2004 / 018089. Each MTP reactor includes 6 catalyst beds, and there is a side line cold DME / methanol feed between the upper and lower beds to control the temperature rise of each catalyst layer to be the same (about 10°C). The temperature of the inlet bed is 470°C, and the outlet bed is 480°C. After the cold DME / methanol is fed between the layers and cooled, it enters the next layer. The reactor of the present invention is now used, and a water-cooled or heat-exchange coiled radial reactor is used to set up 7 insulation layers and 6 heat exchange layers in layers, and 6 steam drums are equipped to form 6 circuits. The ZAPO-34MTP catalyst of Shanghai Petrochemical Research Institute is used, and the drum pressure is adjusted to control the adiabatic reaction at 450℃ in the adiabatic layer and the heat exchange reaction at 460℃ in the heat exchange layer. Under the same device scale, the catalyst loading factor of the reactor is increased from about 25% of the Lurgi segmented cold shock tower to 75%, and the reactor is greatly reduced from the original diameter of more than 10 meters and the height of more than 30 meters. At the same time, the cooling of the raw materials between the adiabatic sections is changed to indirect heat exchange cooling by water-cooled cold pipes, which avoids the dilution of the reaction products, greatly improves the reaction efficiency, saves energy consumption, and reduces production costs. In addition, it can be used for the dehydration of methanol to make gasoline at 310-430℃ with ZSM-5 catalyst.

[0056] The stable temperature control of any reactor is the key to the successful and efficient operation of the reactor. The coolant used to adjust the reactor temperature must meet the following requirements: ① good chemical stability; ② large specific heat capacity, high latent heat of vaporization, etc. Due to the good chemical stability, high specific heat capacity and large heat of vaporization of water, water is the most commonly used coolant. In the production process, the by-product water vapor can be used to recover heat. However, mineral oil is required at temperatures above 300°C. Mineral oil has a low vapor pressure, but poor thermal stability, small specific heat capacity and low flash point, so it is not widely used. Biphenyl or biphenyl-biphenyl ether is a heat transfer oil with good chemical stability. It is generally used in small-scale occasions. The molten salt vapor pressure is lower and can be operated at higher temperatures. It is mostly used in high-temperature occasions above 400°C. The disadvantage is that it is highly corrosive.

[0057] As can be seen from the above embodiments, the present invention can be used in a high-temperature catalytic fixed-bed reactor at a temperature of >300°C to produce high-temperature and high-pressure steam as a by-product in a high-temperature reactor, just like the shell-and-tube reactor with a catalyst installed in the tube, which is currently widely used for medium and low temperature reactions. For example, Examples 1 to 4 are used for ammonia synthesis, and Example 5 is used for methanation of synthesis gas to produce artificial natural gas LNG. The reactor and the external by-product steam boiler are combined into one, which is used for dehydration of methanol to produce propylene MTP. The by-product steam in the reactor is quenched by cold air instead of the raw material methanol, which greatly simplifies the process, saves investment, reduces energy consumption, and has significant economic benefits compared with the existing foreign advanced technology.

[0058] The embodiments and contents listed in the patent application are based on the premise that the cooling medium heat exchange reaction zone and the adiabatic reaction zone are arranged at intervals in the tube of the reactor. The specific equipment and process parameters are not limited to this specification. For example, the heat exchange tube can be a spirally wound tube, a straight tube or a heat exchange plate. The number of heat exchange zones and the outlet area of ​​the reaction zone may be provided with an insulating layer, or may not be provided and a heat exchange layer may be used. The gas may flow from the outside to the inside in a centrifugal flow, or may be centrifugal or water circulated from the inside to the outside. Forced circulation may be achieved by a pump, or natural circulation may be achieved without a pump.

Claims

1. A temperature-optimized reactor, comprising a shell, heat exchange internals consisting of a heat exchange tube bundle, and a catalyst basket with a porous gas distribution plate, wherein the center of the catalyst basket is provided with a porous gas collecting pipe or a porous gas distribution pipe, and the shell is provided with a reaction gas inlet and outlet, a catalyst loading and unloading port, a manhole, a heat exchange tube bundle water inlet pipe box, and a water vapor outlet pipe box, characterized in that: The inner basket of the catalyst basket is provided with a heat exchange zone composed of multiple rows of heat exchange tubes distributed according to the cross section, and an insulation zone without heat exchange tubes is provided between the inner and outer heat exchange zones. The heat exchange zone and the insulation zone are separated by a porous annular sleeve and arranged in concentric ring intervals. The two ends of the heat exchange tubes of the multiple concentric ring heat exchange zones are respectively connected to the water inlet pipe box and the water outlet steam pipe box. The water inlet pipe box and the water outlet steam pipe box are connected in series with a single steam drum with a steam pressure regulating pipeline directly or through a circulating water pump to form a circulation loop. The temperature of each layer of each heat exchange zone and the insulation zone is independently adjusted by adjusting the vaporization pressure of the heat exchange medium to adjust the vaporization temperature; The heat exchange tubes in the heat exchange zone are spirally wound tubes.

2. A process using the reactor as claimed in claim 1, characterized in that: The synthesis gas is heated by the heat exchanger and then enters the reactor for reaction. The reactor is externally connected to a circulation loop including a steam drum. The high temperature generated by the reaction gas during the reaction heats the heat exchange medium to generate steam. The gas after the reaction exits the reactor and exchanges heat with the synthesis gas before entering the tower. It then passes through an air cooler and a water cooler or a water cooler and an ammonia cooler, and then is separated into gas and liquid in a gas-liquid separator.

3. The process according to claim 2, characterized in that: The process method is used for ammonia synthesis, adopts low pressure and isobaric ammonia synthesis technology for preparing synthesis gas from coal or residual oil, and the ammonia synthesis pressure is ≤22MPa.

4. The process according to claim 3, characterized in that: The ammonia synthesis pressure is ≤18MPa.

5. The process according to claim 2, characterized in that: The process is used for ammonia synthesis, using ferrous, ferrous or ferrous-cobalt or ruthenium-based ammonia synthesis catalyst, with a maximum catalytic temperature of <480°C.

6. The process according to claim 3, characterized in that: The circulation ratio of the ammonia synthesis circulating gas volume to the raw material gas volume is <2.5, and the synthesis purge gas is separated by a membrane to recover effective hydrogen.

7. The process according to claim 2, characterized in that: The process method is used to produce methane from synthesis gas, using isobaric methanation at the same pressure as the raw synthesis gas or high-pressure methanation at >5MPa.

8. The reactor according to claim 1, characterized in that: The reactor is used for high-temperature fixed-bed gas-solid phase catalytic reaction of methanol dehydration to produce olefins and gasoline, namely MTP, MTO, MTG, at a reaction temperature of >300°C, and o-xylene oxidation to produce phthalic anhydride.

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