Integrated methanol reforming hydrogen production reactor
By combining the methanol reformer with the evaporator and setting a strengthened heat transfer structure at the front end of the reaction tube, the problems of difficulty in maintaining the catalyst temperature and low structure in the prior art are solved, and efficient methanol reforming and hydrogen production reaction are achieved .
Patent Information
- Application Number
- CN202420890234.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-26
- Publication Date
- 2025-02-18
- Estimated Expiration
- 2034-04-26
AI Technical Summary
When maintaining the optimal reaction temperature range of the catalyst, the existing methanol reformer system has high power consumption, difficult component selection, low structure and low reaction efficiency.
Design an integrated methanol reforming hydrogen production reactor, combine the reformer with the evaporator, heat the methanol water vapor to the optimal reaction temperature through the methanol water evaporation part, and set up a strengthened heat transfer structure at the front end of the reaction tube to improve the Heat transfer efficiency.
It achieves a more compact structure and smaller volume, reduces heat loss, improves overall efficiency, ensures catalyst reaction efficiency, and reduces the temperature difference between front and back of the reforming side reaction tube.
Smart Images
Figure CN222498685U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of methanol reformers, in particular to an integrated methanol reforming hydrogen production reactor. Background Art
[0002] A methanol reformer is a device used in chemical engineering, especially in the field of fuel cell technology, which can produce hydrogen for hydrogen fuel cells or other hydrogen-using scenarios through the reaction of a mixture of methanol and water (steam). Methanol is converted into hydrogen and carbon dioxide through the combined action of pressure, heat and catalysts, and high-purity hydrogen can then be extracted through methods such as pressure swing adsorption (PSA) or separation membranes.
[0003] The optimal reaction temperature range of the reforming catalyst used in the conventional methanol reformer system is 350±25℃. In the prior art, the following method is usually used to maintain the reforming catalyst in the optimal reaction temperature range during the reforming reaction: two sets of heat sources are used, one of which is used to heat the flue gas flow channel of the reformer. Due to the reaction temperature range limit of the catalyst, the temperature of the hot flue gas cannot be too high, otherwise the catalyst will irreversibly lose its activity due to overheating. On this basis, in order to ensure the heat supply, it can only be compensated by increasing the flue gas flow rate, resulting in high system power consumption and difficulty in component selection; at the same time, since the remaining tail gas heat is not enough to raise the temperature of methanol water to the reaction temperature in advance, another set of heat source and heat exchanger or evaporator is required to heat the methanol water to the optimal reaction temperature range. If another set of heat source is not set to heat the methanol water, and the methanol water is directly introduced into the reformer, the front section of the reformer reaction tube only serves as a reheater, and the catalyst filled in this area does not play a role, which reduces the reaction efficiency of the reformer.
[0004] In addition, more pipes are needed to connect the various functionally independent components, resulting in the overall volume, weight, and system efficiency of the reformer losing their advantages. The manufacturing and assembly process is relatively cumbersome, and independent components also increase the complexity of system control. Too many pipe connections will also increase the risk of system leakage, and there will be a large amount of heat loss and low energy conversion efficiency. Utility Model Content
[0005] The technical problem to be solved by the utility model is to provide an integrated methanol reforming hydrogen production reactor, improve the compactness of the structure, reduce the temperature difference before and after the reforming side reaction tube, and improve the utilization efficiency of the catalyst in the reaction tube.
[0006] The utility model solves the technical problem by adopting the following technical solution: providing an integrated methanol reforming hydrogen production reactor, comprising a shell, a plurality of reforming reaction tubes parallel to each other are arranged in the shell, a methanol water evaporation part is arranged outside the shell, the gaps between the reforming reaction tubes are hot flue gas flow channels, the two ends of the shell are respectively a hot flue gas inlet communicated with the hot flue gas flow channel and a reforming side outlet communicated with the tail end of the reforming reaction tube, the methanol water evaporation part comprises a methanol water vaporization flow channel and a tail gas flow channel adjacent thereto, one end of the methanol water vaporization flow channel is provided with a reforming side methanol water inlet, and the One end of the exhaust flow channel is communicated with the tail end of the hot flue gas flow channel, and the other end is provided with a flue gas exhaust outlet. The inlet end of the reforming reaction tube is provided with a reaction tube end face connecting plate, and the reaction tube end face connecting plate includes an inner plate and an outer plate. A transfer cavity communicated with the tail end of the methanol aqueous solution vaporization flow channel is provided between the inner plate and the outer plate, and the transfer cavity is communicated with the reforming reaction flow channel in the reforming reaction tube. The reforming reaction tube is filled with a carrier coated with a reforming catalyst or reforming catalyst particles, and the hot flue gas inlet is communicated with the hot flue gas flow channel through a flue gas input hole that penetrates the reaction tube end face connecting plate.
[0007] Preferably, a heat insulation layer is provided between the outer surface of the shell and the methanol-water evaporation section.
[0008] Preferably, flow equalizing plates and deflector plates are equidistantly arranged in the hot flue gas flow passage.
[0009] Preferably, a layer of flue gas flow channel is respectively provided on both sides of the methanol-water solution vaporization flow channel, and the tail end of the flue gas flow channel is communicated with the flue gas tail gas outlet surrounding the hot flue gas inlet.
[0010] Preferably, a heat transfer enhancement structure is provided on the outer wall surface of the input end of the reforming reaction tube.
[0011] Preferably, the heat transfer enhancement structure is a plurality of fins arranged around the front end outer wall of the reforming reaction tube.
[0012] Beneficial Effects
[0013] The prior art requires that a relatively low-temperature hot flue gas with a large flow rate and a temperature only slightly higher than the optimal reaction temperature of the catalyst of 350±25°C be input into the flue gas flow duct. After adopting the integrated methanol reforming hydrogen production reactor provided by the utility model, the temperature of the hot flue gas input into the flue gas flow duct can be increased to 600±50°C and the required flow rate can be effectively reduced. The hot flue gas tail gas after passing through the flue gas flow duct will be cooled to about 350°C. The hot flue gas tail gas after heat exchange in the reformer is passed into the evaporator layer, which is sufficient to heat and vaporize the methanol water vapor to 125±15°C. The methanol water vapor after preliminary vaporization is heat-exchanged with the high-temperature hot flue gas for secondary heating, so that the methanol water vapor reaches the optimal reaction temperature range of 350±25°C before contacting the catalyst, thereby ensuring the reaction efficiency of the catalyst and promoting the rapid progress of the reforming reaction.
[0014] The utility model combines the reformer and the evaporator together. On the premise of ensuring the amount of hydrogen produced, only one set of heat sources needs to be provided for the flue gas flow passage of the reforming reactor. The structure is more compact and the volume is smaller, which reduces heat loss, thereby improving the overall efficiency and facilitating temperature control of the reforming reactor. By arranging an enhanced heat transfer structure at the front end of the reaction tube, the high-temperature flue gas just entering the shell side of the reformer is diffused to the front section and the middle section of the reaction tube more quickly and evenly, preventing high accumulation in the front section of the reforming reaction tube, reducing the front end temperature, reducing the temperature difference between the front and rear of the reaction tube on the reforming side, and eliminating the destructive damage of the reforming catalyst caused by the high inlet temperature. BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 This is a cross-sectional view of the structure of an integrated methanol reforming hydrogen production reactor.
[0016] Figure 2 for Figure 1 Enlarged schematic diagram of the methanol-water evaporation section.
[0017] Figure 3 This is a schematic diagram of the flow channel connection of an integrated methanol reforming hydrogen production reactor.
[0018] Among them, A-hot flue gas inlet; B-flue gas outlet; C-methanol water inlet on the reforming side; D-reforming side outlet;
[0019] 1- flue gas and tail gas confluence cavity; 2- reforming reaction tube end connection plate; 3- flow equalizing plate; 4- reforming reaction tube; 5- baffle; 6- reformer methanol water inlet pipe; 7- enhanced heat transfer structure; 8- thermal insulation layer; 9- methanol water solution vaporization flow channel; 10- tail gas flow channel; 11- hot flue gas flow channel.
[0020] The same reference numerals in the various drawings represent the same components. DETAILED DESCRIPTION
[0021] The present invention is further described below in conjunction with specific embodiments. It should be understood that these embodiments are only used to illustrate the present invention and are not used 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 make various changes or modifications to the present invention, and these equivalent forms also fall within the scope defined by the claims attached to this application.
[0022] like Figure 3 As shown, the utility model provides an integrated methanol reforming hydrogen production reactor, including a shell, wherein a plurality of reforming reaction tubes parallel to each other are arranged in the shell, the shell is covered with a methanol water evaporation part, the gaps between the reforming reaction tubes are hot flue gas flow channels, the two ends of the shell are respectively a hot flue gas inlet communicated with the hot flue gas flow channel and a reforming side outlet communicated with the tail end of the reforming reaction tube, the methanol water evaporation part includes a methanol water vaporization flow channel and an exhaust gas flow channel adjacent thereto, one end of the methanol water vaporization flow channel is provided with a reforming side methanol water inlet, and the exhaust gas flow channel is provided with a methanol water vaporization flow channel at the rear end thereof. One end is communicated with the tail end of the hot flue gas flow channel, and the other end is provided with a flue gas exhaust outlet. The inlet end of the reforming reaction tube is provided with a reaction tube end face connecting plate, and the reaction tube end face connecting plate includes an inner plate and an outer plate. A transfer cavity communicated with the tail end of the methanol aqueous solution vaporization flow channel is provided between the inner plate and the outer plate, and the transfer cavity is communicated with the reforming reaction flow channel in the reforming reaction tube. The reforming reaction tube is filled with a carrier coated with a reforming catalyst or reforming catalyst particles, and the hot flue gas inlet is communicated with the hot flue gas flow channel through a flue gas input hole that penetrates the reaction tube end face connecting plate.
[0023] By adopting the integrated methanol reforming hydrogen production reactor provided by the utility model, the hot flue gas tail gas after heat exchange in the reformer is passed into the evaporator layer, the methanol aqueous solution is heated and vaporized, and the vaporized methanol water vapor is heated twice to the required reaction temperature when passing through the enhanced heat transfer section, so that the methanol water vapor reaches the optimal reaction temperature range before contacting the catalyst, and the reforming reaction is promoted to proceed quickly. The reformer is combined with the evaporator and the reheater. On the premise of ensuring the hydrogen production amount, the structure is more compact and the volume is smaller, and the heat loss is reduced, thereby improving the overall efficiency.
[0024] A heat insulation layer is provided between the outer surface of the shell and the methanol-water evaporation section to prevent the reforming reaction zone in the high temperature section from directly contacting the evaporator layer in the low temperature section, which would interfere with the heat transfer on both sides, thereby improving the accuracy of overall temperature control, reducing the control difficulty, reducing heat loss in the reforming reaction zone, and improving heat transfer efficiency.
[0025] The hot flue gas flow passage is equidistantly arranged with flow equalizers and baffles. The flow equalizer evenly distributes the hot flue gas on the cross section of the reformer shell side, and the baffle increases the flow length of the hot flue gas entering the shell side, increases the heat transfer time between the hot flue gas and the reaction tube, and increases the effective heat transfer.
[0026] A layer of flue gas flow channel is provided on both sides of the methanol-water vaporization flow channel, and the tail end of the flue gas flow channel is connected to the flue gas tail gas outlet surrounding the hot flue gas inlet. The heating area of the methanol-water vaporization flow channel is increased by sandwiching, thereby improving the heat generation efficiency.
[0027] The outer wall surface of the input end of the reforming reaction tube is provided with a section of enhanced heat transfer structure. The enhanced heat transfer structure is a plurality of fins arranged around the outer wall of the front end of the reforming reaction tube. In other embodiments, it can also be a grid or other structure that increases the contact area between the outer wall of the reforming reaction tube and the hot flue gas in the hot flue gas flow channel to achieve rapid heat exchange at the front end.
[0028] like Figure 1 , 2 As shown, in a specific embodiment, the shell is a cylindrical shell, and the plurality of methanol-water evaporation parts are arranged in a ring shape, and the circumference is evenly distributed outside the shell. The reforming reaction tubes are arranged in parallel inside the shell, and the front end of the hot flue gas flow channel is a reaction tube end surface connection plate, followed by a flow equalizing plate, and then a plurality of flow equalizing plates are set up in sequence. The front end of the enhanced heat transfer structure is connected to the inner plate, and the end is located between the first baffle and the first flow equalizing plate at the front end. The reforming catalyst is arranged at the rear end of the enhanced heat transfer structure.
Claims
1. An integrated methanol reforming hydrogen production reactor, comprising a shell, characterized in that: The shell is provided with a plurality of reforming reaction tubes parallel to each other, and the shell is covered with a methanol-water evaporation part. The gaps between the reforming reaction tubes are hot flue gas flow passages, and the two ends of the shell are hot flue gas inlets communicating with the hot flue gas flow passages and reforming side outlets communicating with the tail ends of the reforming reaction tubes. The methanol-water evaporation section comprises a methanol-water vaporization flow channel and an adjacent tail gas flow channel, one end of the methanol-water vaporization flow channel is provided with a reforming-side methanol-water inlet, one end of the tail gas flow channel is communicated with the tail end of the hot flue gas flow channel, and the other end is provided with a flue gas tail gas outlet. The inlet end of the reforming reaction tube is provided with a reaction tube end surface connection plate, the reaction tube end surface connection plate includes an inner plate and an outer plate, a transfer cavity communicating with the tail end of the methanol aqueous solution vaporization flow channel is provided between the inner plate and the outer plate, the transfer cavity is communicated with the reforming reaction flow channel in the reforming reaction tube, and the reforming reaction tube is filled with a carrier coated with a reforming catalyst or reforming catalyst particles, The hot flue gas inlet is communicated with the hot flue gas flow channel through a flue gas input hole penetrating the reaction tube end surface connection plate.
2. The integrated methanol reforming hydrogen production reactor according to claim 1, characterized in that: A heat insulation layer is provided between the outer surface of the shell and the methanol-water evaporation portion.
3. The integrated methanol reforming hydrogen production reactor according to claim 1, characterized in that: Flow equalizing plates and deflector plates are equidistantly arranged in the hot flue gas flow passage.
4. The integrated methanol reforming hydrogen production reactor according to claim 1, characterized in that: A layer of flue gas flow channel is respectively arranged on both sides of the methanol-water vaporization flow channel, and the tail end of the flue gas flow channel is communicated with the flue gas tail gas outlet surrounding the hot flue gas inlet.
5. The integrated methanol reforming hydrogen production reactor according to claim 1, characterized in that: The outer wall surface of the input end of the reforming reaction tube is provided with a section of enhanced heat transfer structure.
6. The integrated methanol reforming hydrogen production reactor according to claim 5, characterized in that: The heat transfer enhancement structure is a plurality of fins arranged around the front end outer wall of the reforming reaction tube.