Electrically-driven reactor based on conductive heating integral honeycomb structure and application of electrically-driven reactor

Abstract

The invention discloses an electrically driven reactor based on a conductive heating integral honeycomb structure, which comprises a cylinder, an integral honeycomb structure heater capable of generating Joule heat under a power-on condition is arranged in the cylinder, the honeycomb structure heater is cylindrical, longitudinal fluid channels which are regularly arranged are formed in the honeycomb structure heater, and catalyst particles are filled in the channels; a thermal insulation material is filled between the outer wall of the honeycomb structure heater and the inner wall of the cylinder body; an upper sealing head and a lower sealing head are respectively arranged at the upper end and the lower end of the cylinder body; a gas distributor is arranged between the upper sealing head and the cylinder body, and a catalyst supporting plate is arranged between the lower sealing head and the cylinder body; a strip-shaped drainage conductor is arranged on the outer wall of the honeycomb structure heater and is led out of the reactor through a wire interface to be connected with an external power supply. The invention also discloses an application of the electrically driven reactor. The electrically-driven reactor is simple in structure, convenient to operate, energy-saving, environment-friendly and beneficial to popularization and application in production practice.

Description

Technical Field

[0001] The invention belongs to the technical field of reactor design, and in particular relates to an electric-driven reactor based on a conductive heating integral honeycomb structure and an application thereof. Background Art

[0002] Methane reforming technology is an important industrial chemical process for producing hydrogen and carbon monoxide. This technology is widely used in petrochemical, ammonia synthesis, fuel cells and other fields. The basic process of methane reforming is to convert methane and one or more of water vapor, carbon dioxide and oxygen into hydrogen and carbon monoxide through a catalyst at high temperature. Common methane reforming processes include steam reforming, carbon dioxide reforming, combined reforming and tertiary reforming. The methane reforming process is highly endothermic, so sufficient heat must be supplied to the reactor to meet the reaction requirements. However, methane reforming usually needs to be carried out under high temperature conditions. The unreasonable temperature distribution in the reactor is particularly prone to carbon deposition, which can easily cause catalyst sintering and deactivation, affecting the long-term stable operation of the device.

[0003] For the conventional shell-and-tube reactor commonly used in reforming reactions, heat is transferred to the catalyst and reaction gas by radiation and convection through the reactor wall, and the thermal energy utilization efficiency is relatively low. Due to its endothermic reaction characteristics, the temperature distribution inside the reaction tube is uneven, that is, the bed temperature near the wall is much higher than the center temperature, resulting in low heat transfer efficiency and poor energy utilization inside the reactor. In order to improve the reaction conversion rate, it is necessary to increase the temperature of the outer wall of the reaction tube so that the center of the bed meets the reaction temperature, but the bed close to the outer wall of the reaction tube is prone to local high temperature, resulting in carbon deposition on the catalyst and sintering deactivation. Therefore, maintaining a uniform temperature distribution inside the reactor and preventing high-temperature areas from appearing in local areas inside the reactor have gradually become a hot spot in endothermic reaction technologies such as methane reforming. In view of the shortcomings of the prior art, it is necessary to develop a reactor with a simple and compact structure, uniform heat distribution, high energy utilization and easy operation.

[0004] CN113301981A discloses a conductive honeycomb body, comprising a plurality of intersecting porous walls arranged to provide a pore matrix. The invention is applied to a catalytic reaction system, and the wall surface must be coated with a catalyst, which is a complex process and is easy to fall off during use, resulting in high maintenance costs in the later stage.

[0005] CN103204464A discloses a honeycomb oxygen carrier reactor for chemical chain reforming of methane, including a reactor body, wherein the reactor body includes an outer wall and an external heating cylinder, and a honeycomb oxygen carrier is formed in the outer wall and the external heating cylinder. The main purpose of the invention is to use a honeycomb oxygen carrier reactor to carry out chemical chain reforming of methane to produce synthesis gas, and to transfer lattice oxygen and heat to methane through the oxygen carrier, without the need for pure oxygen preparation, and without the need to drive the rapid circulation of solid particles, so as to achieve mild operating conditions and isothermal operation. However, the reactor of the invention still requires outer wall heating, and the scale of heat transfer inside the reactor is large; the reaction process does not require a catalyst, and the honeycomb oxygen carrier is integrally formed after high-temperature pressing and sintering, which is more complicated than directly filling catalyst particles; and fuel reforming, gas purging, and air regeneration steps are required during operation, which are complicated to operate and have low efficiency, and there are still great difficulties in actual industrial application.

[0006] Therefore, for actual industrial applications, requirements such as simple operation, long life and low maintenance cost still need to be met. Summary of the invention

[0007] The purpose of the present invention is to overcome the defects of the external wall heating reactor in the prior art, such as uneven internal temperature distribution, low heat transfer efficiency, low heat utilization rate and inconvenient operation, so as to provide an electrically driven reactor based on a conductive heating integral honeycomb structure.

[0008] To achieve the above-mentioned purpose, the first aspect of the present invention provides an electrically driven reactor based on a conductive heating integral honeycomb structure, comprising a cylinder, an integral honeycomb structure heater generating Joule heat under power-on conditions is arranged inside the cylinder, the integral honeycomb structure heater is cylindrical, and a plurality of regularly arranged longitudinal fluid channels are formed inside the cylinder, and the fluid channels are filled with catalyst particles; the outer wall of the integral honeycomb structure heater and the inner wall of the cylinder are filled with insulation material; the upper and lower ends of the cylinder are respectively provided with an upper head and a lower head, and the upper head is provided with a gas inlet, and the lower head is provided with a gas outlet; a gas distributor is provided between the upper head and the cylinder, and a catalyst support plate is provided between the lower head and the cylinder; a strip-shaped drainage conductor is provided on the outer wall of the integral honeycomb structure heater, and a corresponding wire interface is provided on the cylinder at a position corresponding to the strip-shaped drainage conductor, and the strip-shaped drainage conductor is led out of the reactor through the wire interface through a wire to connect with an external power source.

[0009] According to the present invention, the cross section of the fluid channel is a regular triangle, a regular quadrilateral or a regular hexagon, and all the fluid channels have the same wall thickness.

[0010] According to the present invention, the shape of the catalyst particles filled in the fluid channel is selected from a combination of one or more of spheres, cylinders, Raschig rings, four-hole columns, and seven-hole columns.

[0011] Preferably, the catalyst particles are randomly stacked from the bottom of each fluid channel to the top of the fluid channel.

[0012] According to the present invention, the material of the integral honeycomb structure heater is selected from Fe, Cr, Ni, Cu, Al, Co, Si or their alloys; the material of the strip-shaped drainage conductor is selected from Fe, Cr, Ni, Cu, Al, Co, Si or their alloys, and the resistivity is lower than the material of the integral honeycomb structure heater.

[0013] According to the present invention, the upper end of the thermal insulation material is higher than the upper surface of the integral honeycomb structure heater, thereby forming a reactor cavity between the honeycomb structure heater and the gas distributor; the lower end of the thermal insulation material is flush with the lower end of the cylinder and the lower end of the integral honeycomb structure heater.

[0014] According to the present invention, the gas distributor is in the shape of a disc matching the inner wall of the cylinder, the outer edge of its lower surface is against the upper surface of the insulation layer, and the middle area corresponding to the reactor cavity is provided with regularly arranged pores allowing gas to pass through; preferably, the pores are circular channels, and the arrangement shape of the pores is circular.

[0015] According to the present invention, the catalyst support plate abuts against the bottom ends of the integral honeycomb structure heater and the thermal insulation material, and the contact area between the catalyst support plate and the bottom end of the integral honeycomb structure heater is provided with dense pores.

[0016] According to the present invention, the material of the thermal insulation material is selected from one or more combinations of glass wool, rock wool, aluminum silicate, and composite silicate.

[0017] The second aspect of the present invention provides the application of the above-mentioned electrically driven reactor based on the conductive heating integral honeycomb structure, which is used in a reactor of an endothermic reaction system of methane steam / dry gas reforming or methane combined / triple reforming.

[0018] The present invention has the following beneficial effects:

[0019] 1. The electric driven reactor of the present invention uses electric heating instead of traditional fuel oil heating, which reduces carbon dioxide emissions and the footprint of the device; by arranging an integral honeycomb structure heater in the cylinder, it can respond quickly when powered on and reach the reaction temperature in a short time, saving start-up time.

[0020] 2. By filling the slender fluid channel of the integral honeycomb structure heater with catalyst particles, the heat transfer path is effectively shortened. The continuous heating of the outer wall of the fluid channel and the uniform heat supply can reduce local overheating, further improving the heat transfer efficiency and energy utilization, making the reaction more complete and avoiding the reduction of reaction efficiency due to uneven temperature.

[0021] 3. The electrically driven reactor based on the conductive heating integral honeycomb structure of the present invention has a simple structure, is easy to operate, and is energy-saving and environmentally friendly, which is conducive to its popularization and application in production practice. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a cross-sectional schematic diagram of an electrically driven reactor based on a conductive heating integral honeycomb structure of the present invention.

[0023] Figure 2 for Figure 1 Schematic diagram of the gas distributor in .

[0024] Figure 3 A and 3B are the structural schematic diagram and cross-sectional schematic diagram of the electrically driven heater and the spherical catalyst particles filled in the channel in Example 1, respectively.

[0025] Figure 4 A and 4B are respectively a schematic diagram of the structure and a schematic diagram of the cross section of the electrically driven heater and the Raschig ring catalyst particles filled in the channel in Example 2.

[0026] Figure 5 A and 5B are respectively a schematic diagram of the structure and a schematic diagram of the cross section of the electrically driven heater and the seven-hole column catalyst particles filled in the channel in Example 3. DETAILED DESCRIPTION

[0027] The present invention will be further described below by specific examples in conjunction with the accompanying drawings. It should be understood that these examples are only used to illustrate the present invention and are not intended to limit the scope of the present invention. In addition, it should be understood that after reading the content taught by the present invention, those skilled in the art can determine the specific process conditions according to the principles and embodiments disclosed in the present invention, as well as the purposes of the relevant process flow and the common knowledge in the art. The process equipment or devices not specifically noted in the following examples all adopt conventional equipment or devices in the art.

[0028] In the description of the present application, it should be understood that if the terms "upper", "lower", "top", "bottom", "upper end", "lower end", "thickness" and the like appear, the orientation or position relationship indicated by these terms is based on the orientation or position relationship shown in the drawings, which is only for the convenience of describing the present application and simplifying the description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present application.

[0029] Example 1

[0030] This embodiment provides an electrically driven reactor based on a conductive heating monolithic honeycomb structure, which is suitable for endothermic reaction systems such as methane steam / dry gas reforming, methane combined / triple reforming, etc. Figure 1 As shown, the electrically driven reactor comprises a cylinder 4, inside of which is arranged an integral honeycomb structure heater 9 which generates Joule heat when powered on, the honeycomb structure heater 9 being cylindrical, and having a plurality of longitudinal elongated fluid channels 12 arranged regularly formed therein, the fluid channels 12 being filled with catalyst particles 10; between the outer wall of the honeycomb structure heater 9 and the inner wall of the cylinder 4 is filled an insulating material 13, for preventing the Joule heat generated by the honeycomb structure heater 9 from exchanging heat with the environment through the wall of the cylinder 4 and causing heat loss; the cylinder An upper end and a lower end of 4 are provided with an upper head 2 and a lower head 5 respectively, and a gas inlet 1 is provided on the upper head 2, and a gas outlet 6 is provided on the lower head 5; a gas distributor 3 is provided between the upper head 2 and the cylinder 4 for optimizing the gas flow distribution, and a catalyst support plate 8 is provided between the lower head 5 and the cylinder 4; a strip-shaped drainage conductor 11 is provided on the outer wall of the honeycomb structure heater 9, and a corresponding wire interface 7 is provided on the cylinder 4 at a position corresponding to the strip-shaped drainage conductor 11, and the strip-shaped drainage conductor 11 is led out of the reactor through the wire interface 7 through a wire and connected to an external power supply.

[0031] In this embodiment, the diameter of the cylinder 4 is preferably 300 mm to 600 mm.

[0032] The cross section of the fluid channel 12 is a regular triangle, a regular quadrilateral or a regular hexagon. In this embodiment, the cross section of the fluid channel 12 is a regular hexagon with a side length of 30 mm to 60 mm and a length of 1000 to 1500 mm. Figure 3 A and Figure 3 As shown in B; preferably, all fluid channels 12 have the same wall thickness, and a DC power source passes through the honeycomb structure heater 9 to form a uniform current distribution; the Joule heat power generated by all outer walls of the fluid channel 12 is the same, and the overall temperature reaches above 1000°C.

[0033] The shape of the catalyst particles 10 filled in the fluid channel 12 is selected from a combination of one or more of sphere, cylinder, Raschig ring, four-hole column, and seven-hole column. In this embodiment, the catalyst particles are spherical, and the particle size is 10 mm to 20 mm. The catalyst particles 10 are randomly stacked from the bottom of each fluid channel 12 to the top of the fluid channel 12, and part of the outer wall of the catalyst particles 10 is close to the heat-generating inner wall of the fluid channel 12.

[0034] The specific structural design of the fluid channel 12 inside the above-mentioned honeycomb structure heater 9 and the specific filling method of the catalyst particles 10 ensure that the thermal conductivity performance of each fluid channel 12 is consistent, which helps to form a uniform heat distribution inside the integral honeycomb structure heater 9, avoid local heat accumulation or loss, and thus improve the energy transfer efficiency.

[0035] The current distribution in the integrated honeycomb structure heater 9 is governed by Ohm's law. Under direct current, Ohm's law is defined as:

[0036] U=R·I

[0037] Where U is the electric potential, its unit is V; R is the resistance, its unit is Ω; I is the current, its unit is A.

[0038] When direct current is applied to a three-dimensional geometric structure, the electric field vector E (in V / m) can be written as:

[0039] E=ρ res ·J

[0040] where ρ res is the resistivity, with the unit of Ω·m; J is the current density vector, with the unit of A / m 2 .

[0041]

[0042] Since the resistivity ρ res Due to the intrinsic properties of the material, the resistance R depends only on the geometry of the heater, i.e. the thermal power supplied to an area can be adjusted by varying the cross-sectional area.

[0043] Preferably, the material of the integral honeycomb structure heater 9 is selected from Fe, Cr, Ni, Cu, Al, Co, Si or their alloys. In addition, the integral honeycomb structure heater 9 adopts an integrated manufacturing process, such as 3D printing, extrusion molding or other known processes, to ensure that the heater has good thermal conductivity and mechanical strength.

[0044] Furthermore, the strip-shaped drain conductor 11 is arranged at the top and bottom of the outer wall of the integral honeycomb structure heater 9; preferably, the strip-shaped drain conductor 11 surrounds the honeycomb structure heater 9 at the top and bottom of the outer wall of the honeycomb structure heater 9 and fits closely therewith. The material of the strip-shaped drain conductor 11 has a lower resistivity than that of the integral honeycomb structure heater 9, and the material is selected from Fe, Cr, Ni, Cu, Al, Co, Si or alloys thereof.

[0045] The upper end of the thermal insulation material 13 is higher than the upper surface of the honeycomb structure heater 9, thereby forming a reactor cavity 14 between the honeycomb structure heater 9 and the gas distributor 3; the lower end of the thermal insulation material 13 is flush with the lower end of the cylinder 4 and the lower end of the honeycomb structure heater 9; the material of the thermal insulation material 13 is selected from a combination of one or more of glass wool, rock wool, aluminum silicate, and composite silicate.

[0046] The gas inlet 1 is located at the top of the upper head 2, and the interior of the upper head 2 has a sufficiently large cavity to ensure that the gas entering the reactor can flow fully; the gas outlet 6 is located at the bottom of the lower head 5, and the interior of the lower head 6 has a sufficiently large cavity to ensure that the gas product flows out smoothly and reduce the disturbance of the gas leaving the reactor to the gas distribution in the catalyst bed.

[0047] like Figure 2 As shown, the gas distributor 3 is in the shape of a disc matching the inner wall of the cylinder 4, the outer edge of its lower surface abuts against the upper surface of the thermal insulation layer 13, and the middle area corresponding to the reactor cavity 14 is provided with regularly arranged pores 15 that allow gas to pass through. Preferably, the pores 15 are circular channels, and the arrangement shape of the pores 15 is circular.

[0048] The catalyst support plate 8 is abutted against the bottom end of the integral honeycomb structure heater 9 and the thermal insulation material 13, and the contact area between the catalyst support plate 8 and the bottom end of the honeycomb structure heater 9 is provided with dense pores, so as to support the catalyst particles 10 filled in the honeycomb structure heater 9 and its internal fluid channel 12 while ensuring that the gas in the catalyst bed can pass smoothly but intercepting the catalyst particles from being entrained out of the bed due to gravity and the passage of gas.

[0049] Preferably, the gas distributor 3 and the catalyst support plate 8 are both made of insulating materials and have certain mechanical strength and stability, so as to ensure that the current distribution is not disturbed when the integral honeycomb structure heater is powered on.

[0050] When the electric driven reactor of this embodiment is used for methane combined reforming, the reactant gas preheated and treated in the reactor front end process enters the reactor from the gas inlet 1 at the top of the upper head 2, fully flows in the cavity inside the upper head 2, and enters the catalyst bed inside the honeycomb structure heater 9 after further optimizing the gas flow distribution by the gas distributor 3, and reacts with the catalyst particles in the fluid channel 12. Under the action of uniform Joule heat generated on the fluid channel 12, the catalyst particles 10 effectively catalyze the methane combined reforming reaction, and convert methane, water vapor and carbon dioxide into hydrogen and carbon monoxide in part or in whole. The integral honeycomb structure heater 9 generates Joule heat through direct current, and continues to generate heat in the reactor, thereby ensuring that the temperature in the reactor remains within a preset range. This design helps to maintain uniform heat distribution inside the reactor, reduce the occurrence of side reactions, and further improve the efficiency and energy conversion rate of the methane reforming reaction. The generated hydrogen, carbon monoxide, other products or unreacted gases are discharged from the gas outlet 6 at the bottom of the lower head 5 and are collected and processed.

[0051] When the reaction proceeds for a period of time, due to the formation of carbon deposits on the catalyst, the catalytic activity decreases and the catalyst needs to be regenerated. The gas inlet 1 at the top of the upper head 2 stops introducing the reaction gas and is replaced by introducing the regeneration gas (which is composed of a mixture of one or more gases such as air, oxygen, carbon dioxide, water vapor, hydrogen, etc.). The DC current introduced into the reactor is set to meet the temperature requirement for catalyst regeneration, and the exhaust gas generated in the reaction zone flows out through the gas outlet 6 at the top of the lower head 5.

[0052] Example 2

[0053] The structure and operating conditions of the electrically driven reactor based on the conductive heating integral honeycomb structure of this embodiment are basically the same as those of Example 1. Figure 4 A and Figure 4 As shown in B, the only difference from Example 1 is that the catalyst particles 10 filled in the fluid channel 12 are Raschig ring catalyst particles, and the outer diameter of the Raschig ring catalyst particles is 10mm to 20mm, and the inner diameter is between 5mm and 15mm; the catalyst particles 10 are randomly stacked from the bottom of each fluid channel 12, forming a random stacking structure of elongated Raschig ring catalyst particles in each fluid channel 12.

[0054] The above arrangement is conducive to reducing the amount of catalyst filling in the fluid channel 12, but the line-surface contact between the catalyst particles 10 is conducive to the heat transfer efficiency of the bed in a single fluid channel 12. The special geometric shape of the Raschig ring catalyst particles increases the surface area of ​​the catalyst, thereby promoting full contact between the reaction gas and the catalyst, thereby improving the utilization rate of the catalyst. This design further improves the reaction performance of the overall reactor and ensures a higher conversion rate. The optimized design of the structure enables the reactor to provide a more stable and efficient methane reforming process in industrial applications, thereby meeting higher production requirements.

[0055] Example 3

[0056] The structure and operating conditions of the electrically driven reactor based on the conductive heating integral honeycomb structure of this embodiment are basically the same as those of Example 1. Figure 5 A and Figure 5 As shown in B, the main difference from the embodiment is that the catalyst particles 10 filled in the fluid channel 12 are seven-hole column catalyst particles, the outer diameter of the seven-hole column catalyst particles is 10mm~20mm, and the inner diameter is 2mm~5mm. The catalyst particles are randomly stacked from the bottom of each fluid channel 12, forming a random stacking structure of slender catalyst particles in each fluid channel 12.

[0057] Through the above arrangement, the packing density of the catalyst particles 10 in the fluid channel 12 is increased, and the heat transfer efficiency in a single fluid channel 12 is improved, thereby enhancing the reaction performance of the overall reactor. Since the catalyst particles are densely packed in the fluid channel 12, the reaction gas can more fully contact the catalyst particles 10 when passing through these fluid channels 12, thereby improving the conversion rate of the reaction.

[0058] Example 4

[0059] The operating conditions of the electrically driven reactor based on the conductive heating integral honeycomb structure of this embodiment are consistent with those of Example 1. The main difference between the reactor structure and that of Example 1 is that the fluid channel 12 in the integral honeycomb structure heater 9 is a regular quadrilateral with a side length of 50 mm to 80 mm, the catalyst particles 10 filled in the fluid channel 12 are spherical catalyst particles with an outer diameter of 10 mm to 20 mm, and the catalyst particles are randomly stacked from the bottom of each fluid channel 12, forming an elongated catalyst particle random stacking structure in each fluid channel 12.

[0060] Example 5

[0061] The operating conditions of the electrically driven reactor based on the conductive heating monolithic honeycomb structure of this embodiment are consistent with those of Example 4. The main difference between the reactor structure and that of Example 4 is that the catalyst particles 10 filled in the fluid channel 12 in the monolithic honeycomb structure heater 9 are Raschig ring catalyst particles, the outer diameter of the catalyst particles is 10 mm to 20 mm, the inner diameter is 5 mm to 15 mm, and the catalyst particles are randomly stacked from the bottom of each fluid channel 12, forming an elongated catalyst particle random stacking structure in each fluid channel 12.

[0062] Example 6

[0063] The operating conditions of the electrically driven reactor based on the conductive heating monolithic honeycomb structure of this embodiment are consistent with those of Example 4. The main difference between the reactor structure and that of Example 4 is that the catalyst particles 10 filled in the fluid channel 12 in the monolithic honeycomb structure heater 9 are seven-hole column catalyst particles, the outer diameter of the catalyst particles is 10 mm to 20 mm, the inner diameter is 2 mm to 5 mm, and the catalyst particles are randomly stacked from the bottom of each fluid channel 12, forming an elongated catalyst particle random stacking structure in each fluid channel 12.

[0064] Application Example 1

[0065] This application example is based on Examples 1-3, and all use the same reactor to carry out the methane mixed reforming reaction. Only the catalyst filling structure in the internal fluid channel 12 of the integral honeycomb structure heater 9 is different. It is filled with spherical, Raschig ring and seven-hole column catalyst particles with an outer diameter of 15 mm, respectively. The inner diameters of the Raschig ring and the seven-hole column are 6 mm and 3 mm, respectively. By comparing the effects of different stacking structures of the catalyst particles 10 in the integral honeycomb structure heater 9 on the performance of the reactor, and then comparing it with the traditional fuel oil heated shell and tube reactor, the advantages of the electrically driven reactor based on the conductive heating integral honeycomb structure of the present invention are highlighted. Specifically, the following steps are included:

[0066] 4212L / h methane, 8424L / h water vapor and 1404L / h carbon dioxide are mixed and preheated to 600°C, enter the upper end of the reactor through the gas inlet 1, flow through the upper head 2 from top to bottom, and achieve uniform gas distribution through the gas distribution plate 15. After fully developing through the reactor cavity 14, they enter the bed layer of each fluid channel 12 in the integral honeycomb structure heater 9 to undergo methane combined reforming reaction, and the reaction temperature is 850°C. The fluid channel 12 is a regular hexagon with a side length of 60mm and a length of 1200mm. The reaction gas and generated gas of each fluid channel 12 flow into the lower head 5 through the catalyst support plate 8, and are collected and then discharged through the gas outlet 6.

[0067] Comparative Example 1

[0068] In order to reflect the performance advantages of the electric-driven reactor based on the conductive heating integral honeycomb structure of the present invention, a shell-and-tube reactor heated by traditional fuel oil is used as control 1. The operating conditions including the inlet composition, preheating temperature, catalyst filling amount, reaction temperature and air velocity are the same as those in Examples 1-3, with the difference that: the traditional reactor adopts a shell-and-tube type, the number of pipes is 40, the pipe diameter is 60mm, and the length is 1200mm. The pipes are filled with seven-hole column catalyst particles. The outer diameter of the seven-hole column catalyst particles is 15mm and the inner diameter is 3mm. The heating conditions are fuel oil combustion for heating, and the reactor needs to reserve a fuel combustion cavity.

[0069] The methane and carbon dioxide conversion rates at the outlets of each reactor and the radial temperature difference of the channel in Examples 1-3 and Control 1 are shown in Table 1, respectively.

[0070] Table 1: Conversion rate of methane and carbon dioxide at the outlet and radial temperature difference of the channel

[0071] Methane conversion rate / % Channel radial temperature difference / ℃ Example 1 67.8 20 Example 2 69.3 17 Example 3 70.5 16 Comparison 1 65.2 32

[0072] Application Example 2

[0073] This application example is based on Examples 4-6, and all use the same reactor to carry out the methane mixed reforming reaction. At a reaction temperature of 1150°C, the reactor performance is tested by filling the regular quadrilateral fluid channel 12 inside the integral honeycomb structure heater 9 with catalyst particles 10 of different shapes. The operating conditions are the same as those in Application Example 1, including the inlet composition, catalyst filling amount, inlet temperature and air velocity. The main difference is that the fluid channel 12 is a regular quadrilateral with a side length of 60 mm and a length of 1200 mm. The fluid channels 12 in Examples 4-6 are filled with ball, Raschig ring and seven-hole column catalysts, respectively. The structure and specifications of the catalyst particles are the same as those in Application Example 1.

[0074] Comparative Example 2

[0075] The operating conditions of Comparative Example 2, including the inlet composition, catalyst filling amount, catalyst structure geometry and space velocity, are the same as those of Comparative Example 1. The traditional tubular reactor pipes are filled with seven-hole column catalyst particles as Cui Zhao 2, and the number and specifications of the tubulars are consistent. The main difference is that the gas temperature entering the traditional tubular reactor is preheated to 800°C, and the reaction temperature is 1150°C.

[0076] The methane and carbon dioxide conversion rates at the outlets of each reactor and the radial temperature differences of the channels in Examples 4-6 and Control 2 are shown in Table 2, respectively.

[0077] Table 2: Conversion rate of methane and carbon dioxide at the outlet and radial temperature difference of the channel

[0078] Methane conversion rate / % Channel radial temperature difference / ℃ Example 4 86.8 37 Example 5 87.5 35 Example 6 87.9 34 Comparison 2 83.4 52

[0079] As can be seen from Tables 1 and 2, the electrically driven reactor based on the conductive heating integral honeycomb structure of the present invention has higher methane conversion rate and carbon dioxide conversion rate, which is due to the uniform Joule heat generated by the outer wall of the channel to supply energy to the catalyst. The larger energy supply area and smaller heat transfer path reduce the radial temperature gradient of the catalyst bed in the channel, so that the catalyst is fully utilized and the energy consumption is lower. At the same time, the electrically driven reactor based on the conductive heating integral honeycomb structure of the present invention eliminates the extra volume of the fuel oil combustion cavity, making the reactor more compact.

[0080] The above description is only a detailed description of the preferred embodiments and principles of the present invention. For ordinary technicians in this field, according to the ideas provided by the present invention, there will be changes in the specific implementation methods, and these changes should also be regarded as the protection scope of the present invention.

Claims

1. An electrically driven reactor based on a conductive heating monolithic honeycomb structure, characterized in that: The electrically driven reactor comprises a cylinder (4), wherein an integral honeycomb structure heater (9) generating Joule heat under power-on conditions is arranged inside the cylinder (4), wherein the integral honeycomb structure heater (9) is cylindrical, and a plurality of regularly arranged longitudinal fluid channels (12) are formed inside the integral honeycomb structure heater (9), wherein the fluid channels (12) are filled with catalyst particles (10); a heat-insulating material (13) is filled between the outer wall of the integral honeycomb structure heater (9) and the inner wall of the cylinder (4); an upper end cap (2) and a lower end cap (5) are respectively arranged at the upper end and the lower end of the cylinder (4), and the upper end cap (2) and the lower end cap (5) are respectively provided with a heat-insulating material (13); ... A gas inlet (1) is provided on the head (2), and a gas outlet (6) is provided on the lower head (5); a gas distributor (3) is provided between the upper head (2) and the cylinder (4), and a catalyst support plate (8) is provided between the lower head (5) and the cylinder (4); a strip-shaped drainage conductor (11) is provided on the outer wall of the integral honeycomb structure heater (9), and a corresponding wire interface (7) is provided on the cylinder (4) at a position corresponding to the strip-shaped drainage conductor (11); the strip-shaped drainage conductor (11) is led out of the reactor through the wire interface (7) and connected to an external power source.

2. The electrically driven reactor according to claim 1, characterized in that: The cross section of the fluid channel (12) is an equilateral triangle, a regular quadrilateral or a regular hexagon, and all the fluid channels (12) have the same wall thickness.

3. The electrically driven reactor according to claim 1, characterized in that: The shape of the catalyst particles (10) filled in the fluid channel (12) is selected from a combination of one or more of a sphere, a cylinder, a Raschig ring, a four-hole column, and a seven-hole column.

4. The electrically driven reactor according to claim 1, characterized in that: The catalyst particles (10) are randomly stacked from the bottom of each fluid channel (12) to the top of the fluid channel (12).

5. The electrically driven reactor according to claim 1, characterized in that: The material of the integral honeycomb structure heater (9) is selected from Fe, Cr, Ni, Cu, Al, Co, Si or their alloys, and the material of the strip-shaped drainage conductor (11) is selected from Fe, Cr, Ni, Cu, Al, Co, Si or their alloys, and has a lower resistivity than the material of the integral honeycomb structure heater (9).

6. The electrically driven reactor according to claim 1, characterized in that: The upper end of the thermal insulation material (13) is higher than the upper surface of the integral honeycomb structure heater (9), thereby forming a reactor cavity (14) between the honeycomb structure heater (9) and the gas distributor (3); the lower end of the thermal insulation material (13) is flush with the lower end of the cylinder (4) and the lower end of the integral honeycomb structure heater (9).

7. The electrically driven reactor according to claim 1, characterized in that: The gas distributor (3) is in the shape of a disk that matches the inner wall of the cylinder (4), the outer edge of its lower surface abuts against the upper surface of the thermal insulation layer (13), and a central area corresponding to the reactor cavity (14) is provided with regularly arranged pores (15) that allow gas to pass through; preferably, the pores (15) are circular channels, and the arrangement shape of the pores (15) is circular.

8. The electrically driven reactor according to claim 1, characterized in that: The catalyst support plate (8) abuts against the bottom ends of the integral honeycomb structure heater (9) and the thermal insulation material (13), and a contact area between the catalyst support plate (8) and the bottom ends of the integral honeycomb structure heater (9) is provided with dense pores.

9. The electrically driven reactor according to claim 1, characterized in that: The material of the thermal insulation material (13) is selected from one or more combinations of glass wool, rock wool, aluminum silicate, and composite silicate.

10. Application of an electrically driven reactor based on a conductive heating monolithic honeycomb structure according to any one of claims 1 to 9, characterized in that: Reactor for endothermic reaction system of methane steam / dry gas reforming or methane combined / triple reforming.

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