CN118083911A - Modularized methanol reforming hydrogen production device - Google Patents
Modularized methanol reforming hydrogen production device Download PDFInfo
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- CN118083911A CN118083911A CN202410513770.XA CN202410513770A CN118083911A CN 118083911 A CN118083911 A CN 118083911A CN 202410513770 A CN202410513770 A CN 202410513770A CN 118083911 A CN118083911 A CN 118083911A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 151
- 238000002407 reforming Methods 0.000 title claims abstract description 67
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 29
- 239000001257 hydrogen Substances 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title claims description 11
- 238000006057 reforming reaction Methods 0.000 claims abstract description 73
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims abstract description 57
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 41
- 230000003647 oxidation Effects 0.000 claims abstract description 37
- 230000008016 vaporization Effects 0.000 claims abstract description 37
- 238000009834 vaporization Methods 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 238000001704 evaporation Methods 0.000 claims description 26
- 230000008020 evaporation Effects 0.000 claims description 23
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000005485 electric heating Methods 0.000 claims description 9
- 230000000087 stabilizing effect Effects 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- -1 iron-chromium-aluminum Chemical compound 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 30
- 238000002156 mixing Methods 0.000 abstract description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 21
- 239000003546 flue gas Substances 0.000 description 21
- 239000007789 gas Substances 0.000 description 9
- 230000008859 change Effects 0.000 description 5
- 239000007864 aqueous solution Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
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- 229910001220 stainless steel Inorganic materials 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
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- 230000008569 process Effects 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
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- 238000005516 engineering process Methods 0.000 description 1
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- 238000012360 testing method Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention relates to a modularized methanol reforming hydrogen generator which comprises a reforming reactor, a main heat supply runner, an oxidation reactor, an air inlet and liquid inlet mixing end, a methanol water evaporator, a vaporization cavity runner and an auxiliary heat supply runner, wherein a plurality of reforming reaction pipes are arranged in the reforming reactor, the main heat supply runner is arranged outside the reforming reaction pipes, the oxidation reactor is communicated with the main heat supply runner, and the auxiliary heat supply runner is closely attached to the vaporization cavity runner. The reforming reaction flow channels and the corresponding main heat supply flow channels are divided into a plurality of reforming reaction groups according to the basic temperature in the pipe, the vaporization cavity flow channels and the corresponding auxiliary heat supply flow channels are divided into a plurality of vaporization groups, and the reforming reaction groups and the vaporization groups are in one-to-one correspondence. According to the invention, the vaporization cavity flow channels are arranged on each reforming reaction tube, the reforming reaction flow channels and the vaporization cavity flow channels are grouped, more methanol water is input into the reforming reaction groups with higher average base temperature through the flow equalizing ring, and the flow of each vaporization cavity flow channel is controlled in groups, so that the problem of uneven liquid inlet of each reaction tube on the reforming side of the reformer is solved, and the overall thermal efficiency of the system is effectively improved.
Description
Technical Field
The invention belongs to the technical field of methanol reforming reactors, and particularly relates to a modularized methanol reforming hydrogen production device.
Background
A methanol reformer is a device used in chemical engineering, particularly in the field of fuel cell technology, which can produce hydrogen gas for a hydrogen fuel cell by the reaction of a mixture of methanol and water (steam). Wherein methanol is converted into hydrogen and carbon dioxide by the combined action of pressure, heat and a catalyst, and then high-purity hydrogen can be extracted by a Pressure Swing Adsorption (PSA) or separation membrane method.
In general, in order to improve heat exchange efficiency, the flue gas heating pipes and the methanol reforming reaction pipes are arranged in the methanol reformer in a staggered manner, but because the overall temperature of the flue gas is gradually reduced in the flowing direction, besides the temperature difference in the length direction of the reaction pipes, certain temperature difference is necessarily present due to the influence of gravity and temperature change among the reaction pipes on the same section, the temperature difference in the part can cause the difference of the methanol conversion rate and the hydrogen production rate of the reaction pipes, and the temperature difference in the part can cause the excessive temperature difference of the reformer in severe cases, so that the control strategy of the whole system fails, and the overall conversion rate is reduced rapidly, so that the hydrogen production rate is reduced.
Disclosure of Invention
The invention aims to solve the technical problem of providing a modularized methanol reforming hydrogen production device, which controls the temperature among reforming reaction tubes in a methanol reformer, so that the catalyst in a high-efficiency reaction tube plays a larger role, and the methanol conversion rate in a low-efficiency reaction tube can be kept at a high level.
The technical scheme adopted for solving the technical problems is as follows: the utility model provides a modularization methyl alcohol reforming hydrogen generator, including the inside reforming reactor that is equipped with a plurality of reforming reaction pipes, be located reforming reaction flow path in the pipe of reaction pipe is the tube side, and the main heat supply flow path that is located the pipe is the shell side, reforming reactor's shell side front end communicates with each other with the oxidation reactor, oxidation reactor's front end is equipped with air inlet feed liquor mixed end cover, air inlet feed liquor mixed end cover is equipped with oxidation side methyl alcohol water entry and air inlet, every reforming reaction pipe links to each other with a methyl alcohol water evaporator respectively, reforming reactor includes a plurality of reforming reaction group and corresponding quantity evaporation group, wherein, every reforming reaction group includes the reforming reaction flow path that the foundation temperature is close in a plurality of flow paths, reforming reaction group and evaporation group one-to-one, with the evaporation group that corresponds is used for with the methyl alcohol water is gasified the back input of reforming reaction flow path a plurality of methyl alcohol water evaporator, the methyl alcohol water evaporator links to each other with reforming side methyl alcohol water entry through the flow equalizing ring, the intra-annular is equipped with a plurality of branch ring, the branch ring is as the flow path, every flow path is as the cross-sectional area that the chamber links to each other with the methyl alcohol water entry with the main inlet with the evaporation pipe respectively, the cross-sectional area of the cross-section is big entry with the main pipe respectively.
Preferably, the oxidation side methanol water inlet is provided with a methanol atomizing nozzle.
Preferably, each methanol-water evaporator comprises a vaporization cavity runner and an auxiliary heat supply runner which is tightly attached to the vaporization cavity runner, the vaporization cavity runner and the corresponding auxiliary heat supply runner are divided into a plurality of evaporation groups, the reforming reaction groups are in one-to-one correspondence with the evaporation groups, the front ends of the auxiliary heat supply runners are respectively communicated with the tail ends of a main heat supply runner, the tail ends of the vaporization cavity runners are respectively communicated with the front ends of a reforming reaction tube, and the vaporization cavity runners of the evaporation groups are respectively connected with a reforming side methanol-water inlet through flow equalizing rings.
Preferably, the section of the oxidation reactor is honeycomb, an oxidation catalyst is coated in the oxidation reactor, and the front section of the oxidation reactor is an electric heating device made of iron-chromium-aluminum materials.
Preferably, a sectional type micro-channel carrier is arranged in the reforming reaction tube, and a methanol reforming hydrogen production catalyst is coated in the sectional type micro-channel carrier.
Preferably, the end of the tube side is connected to an outlet manifold module in which a pressure regulating device is arranged.
Preferably, the shell side is provided with flow equalizing plates and baffle plates with alternating sizes in the flowing direction, and the number of the flow equalizing plates and the baffle plates arranged in the reforming reaction group with high average basic temperature is larger than that in the reforming reaction group with low average basic temperature.
Preferably, the methanol water evaporator is circumferentially and uniformly distributed on the outer surface of the reforming reactor.
Advantageous effects
The invention has the following beneficial effects: by arranging one vaporization cavity flow passage for each reforming reaction tube, grouping the reforming reaction flow passages and the vaporization cavity flow passages, inputting more methanol water into the reforming reaction groups with higher average base temperature through the flow equalizing ring, so as to control the flow of each vaporization cavity flow passage, solve the problem of uneven liquid inlet of each reaction tube at the reforming side of the reformer, and further improve the overall heat efficiency of the system on the basis of effectively improving the efficiency of each reforming reaction group; the methanol evaporator is manufactured into an annular module sleeved outside the methanol reactor, so that the problem of overlarge evaporator module is effectively reduced, and the volume of the whole methanol reforming system is reduced; the flue gas side outlet is connected with the methanol evaporator to serve as a heat supply source for methanol water vaporization, and the problem of overhigh temperature of the flue gas side outlet is solved by heat exchange and cooling again, so that the heat efficiency of the system is improved.
According to the invention, the liquid inlets of the reaction tubes are managed in groups, so that the liquid inlet difference among the tubes is adjusted, the liquid inlets of the high-efficiency reaction tubes are more, the liquid inlets of the low-efficiency reaction tubes are less, and the temperature difference among the reaction tubes is reduced in a mode of controlling the reaction degree. The modularized design has compact volume, convenient disassembly and assembly, convenient maintenance, short starting time and low energy consumption, can realize free switching of high power and low power, and has extremely high practical value.
Drawings
FIG. 1 is a front view of a modular methanol reforming hydrogen generator.
Fig. 2 is a cross-sectional view of a modular methanol reforming hydrogen generator of fig. 1.
FIG. 3 is an oxidation side flow diagram of a modular methanol reforming hydrogen generator of FIG. 1.
Fig. 4 is a reforming side flow diagram of a modular methanol reforming hydrogen production unit of fig. 1.
Fig. 5 is a perspective view of the flow equalizing ring in fig. 1.
Fig. 6 is a cross-sectional perspective view of the flow equalizing ring of fig. 5.
Fig. 7 is a front view enlarged diagram of the flow equalization plate in fig. 2.
Wherein, 1-methanol atomizing nozzle; 2-air inlet and liquid inlet mixing end covers; a 3-oxidation reactor; 4-a flue gas tail gas converging cavity; a 5-reforming reactor; 6-methanol water evaporator; 7-a flow equalizing ring; 8-reforming side outlet header module; 9-a male flange; 10-a female flange; 11-V-shaped clamp; 12-a ferrule joint 1; 13-ferrule fitting 2; 14-reforming reaction tubes; 15-reforming reaction flow path; 16-a main heating runner; 17-auxiliary heating flow channels; 18-a flow equalization plate; 19-baffles; 20-vaporizing cavity flow path; 21-an inner ring; 22-middle ring; 23-an outer ring; 24-inlet pipe; 25-outlet pipe; 26-pressure stabilizing cavity.
A-oxidation side methanol water inlet; b-an air inlet; c-an electric heating power interface; d-a tail gas outlet; e-reforming side methanol water inlet; f-reforming side outlet.
Like reference symbols in the various drawings indicate like elements.
Detailed Description
The application will be further illustrated with reference to specific examples. It is to be understood that these examples are illustrative of the present application and are not intended to limit the scope of the present application. Furthermore, it should be understood that various changes and modifications can be made by one skilled in the art after reading the teachings of the present application, and such equivalents are intended to fall within the scope of the application as defined in the appended claims.
The invention provides a modularized methanol reforming hydrogen production device, which comprises a reforming reactor 5, wherein a plurality of reforming reaction pipes are arranged in the reforming reactor, a reforming reaction flow passage positioned in each reforming reaction pipe is a pipe side, a main heat supply flow passage positioned outside each pipe is a shell side, the front end of the shell side of the reforming reactor 5 is communicated with an oxidation reactor 3, the front end of the oxidation reactor 3 is provided with an air inlet and liquid inlet mixed end cover 2, the air inlet and liquid inlet mixed end cover 2 is provided with an oxidation side methanol water inlet A and an air inlet B, and each reforming reaction pipe is respectively connected with a methanol water evaporator 6.
The reforming reactor comprises a plurality of reforming reaction groups and a corresponding number of evaporation groups, wherein each reforming reaction group comprises a plurality of reforming reaction flow channels 15 with similar basic temperatures (smaller temperature differences) in flow channels, the reforming reaction groups are in one-to-one correspondence with the evaporation groups, the evaporation groups corresponding to the reforming reaction groups comprise a plurality of methanol water evaporators 6 for gasifying methanol water and inputting the methanol water into the reforming reaction flow channels 15, the methanol water evaporators 6 are connected with reforming side methanol water inlets E through flow equalizing rings 7, a plurality of split rings are concentrically arranged in the flow equalizing rings 7, the flow equalizing rings are used as pressure stabilizing cavities 26, each pressure stabilizing cavity 26 is respectively connected with an inlet pipe 24 and a plurality of outlet pipes 25 respectively connected with the methanol water evaporators 6, the inlet pipes 24 are connected with reforming side methanol water inlets E provided with a liquid inlet system, and the cross section area of each inlet pipe 24 is larger than the total cross section area of each outlet pipe 25. In other embodiments, the methanol water evaporator may be a large methanol water evaporator of conventional design, and a plurality of methanol water evaporators may be arranged or multiple pipelines may be used to input and output the methanol water evaporator corresponding to the flow equalizing ring.
As shown in fig. 1 and 2, in a specific embodiment, each of the methanol-water evaporators 6 includes a vaporization cavity flow channel 20 and an auxiliary heat supply flow channel closely attached to the vaporization cavity flow channel 20, the vaporization cavity flow channel 20 and the corresponding auxiliary heat supply flow channel are divided into a plurality of vaporization groups, the reforming reaction groups are in one-to-one correspondence with the vaporization groups, the front end of each auxiliary heat supply flow channel is respectively communicated with the tail end of one main heat supply flow channel, the tail end of each vaporization cavity flow channel 20 is respectively communicated with the front end of one reforming reaction tube, and the vaporization cavity flow channels 20 of each vaporization group are respectively connected with the reforming side methanol-water inlet E through the flow equalizing ring 7.
The whole methanol water evaporator 6 is made of aluminum alloy, so that the heat transfer efficiency is ensured. The oxidation side methanol water inlet A is provided with a methanol atomizing nozzle 1. The methanol atomizing nozzle 1 is fixed on the nozzle mounting seat through a nozzle gland and a bolt, wherein the oxidation side methanol water inlet A is arranged on two sides of the air inlet B. The reforming side methanol water inlet E is supplied with liquid through the flow equalizing ring 7. The flow equalizing ring 7 adopts a structure with less inlet and more outlet, and by designing the inlet and outlet pipe diameters of the flow equalizing ring 7, the absolute pressure of 1-5 bar in the cavity of the flow equalizing ring 7 is ensured in the liquid inlet process, so that the resistance formed by gravity and temperature change is overcome, and the liquid inlet uniformity of each vaporizing cavity flow channel 20 is ensured. Meanwhile, according to the temperature distribution and the reaction rate trend in different reaction tubes, the reaction tubes are grouped, and the liquid feeding amount of each grouping is controlled.
In a specific embodiment, as shown in fig. 5 and 6, the methanol water evaporator 6 is divided into three evaporating groups by calculation, and each evaporating group is provided with four evaporating cavity flow passages 20, so that the split rings in the flow equalizing ring 7 are specifically set into an inner ring 21, an intermediate ring 22 and an outer ring 23 which are concentrically arranged, and the three split rings respectively correspond to three different liquid inlet amount requirements of three reforming reaction groups in the reactor. The inner ring 21, the middle ring 22 and the inner ring runner of the outer ring 23 serve as pressure stabilizing cavities 26, each ring is connected with one inlet pipe 24 and four outlet pipes 25, the cross section area of the inlet pipe 24 is larger than the total cross section area of each outlet pipe 25, and the specific size is according to the actual liquid inlet amount and the pressure requirement in the pressure stabilizing cavities 26. The inlet pipe 24 is connected to a reforming side methanol-water inlet E provided with a liquid inlet system, and the outlet pipe 25 is connected to the vaporization cavity flow path 20 of the methanol-water evaporator in the corresponding vaporization group. The liquid inlet system is a conventional pressure stabilizing liquid inlet system, specifically, a pressure sensor, a return pipeline and an electromagnetic valve are arranged between the liquid inlet system and the flow equalizing ring 7, the liquid inlet system conveys methanol aqueous solution to the flow equalizing ring 7, the pressure sensor detects and feeds back pressure, the electromagnetic valve of the return pipeline is cooperated to ensure that the pressure in the pipeline is stable, the pressure in the pressure stabilizing cavity 26 is always higher than an outlet pressure value, and therefore a single loop in the flow equalizing ring 7 is free from the influence of outlet pressure change and gravity, and stable and uniform flow is provided.
The air inlet and liquid inlet mixing end cover 2 is internally provided with a gas-liquid mixer for improving the mixing uniformity of the input methanol water and air.
The section of the oxidation reactor 3 is honeycomb, an oxidation catalyst is coated in the oxidation reactor 3, and the front section of the oxidation reactor 3 is an electric heating device made of iron-chromium-aluminum materials. The electric heating device can be connected with 12-48V direct current through an electric heating power interface C and is used for providing a heat source for cold start of a system, a mixed medium of methanol water and air enters the rear section of the oxidation reactor 3 after the cold start is completed to perform oxidation reaction to further generate heat so as to generate smoke, and an insulating ceramic column is arranged between the front-section electric heating device and the rear-section oxidation reactor 3 to prevent electric leakage.
The reforming reaction tube is internally provided with a sectional type micro-channel carrier with the length of 20-150 mm, and the sectional type micro-channel carrier is internally coated with a catalyst for preparing hydrogen by reforming methanol. The coating thickness of the catalyst for preparing hydrogen by reforming methanol is 5-300 mu m, and the single-carrier catalyst loading capacity is 0.05-1g. The catalyst carrier is loaded according to a specific sequence according to the actual temperature change in the reaction tube and the change trend of the concentration of methanol vapor, and 1-5 carrier types are used simultaneously. The loading principle of the segmented micro-channel carrier is as follows: 1. with the decreasing trend of the concentration of the methanol vapor, the porosity of the catalyst carrier is gradually increased; 2. the catalyst loading amount in the high temperature zone is higher than that in the low temperature zone; 3. the catalyst loading amount in the reaction tube with high heat transfer efficiency is higher than that in the reaction tube with low efficiency.
The end of the tube side is connected with an outlet confluence module which is internally provided with a pressure regulating device.
The auxiliary heat supply flow channel is a tail gas flow channel connected with the flue gas side outlet of the reformer, waste heat of flue gas can be recycled, and the tail end of the auxiliary heat supply flow channel is discharged through a tail gas outlet D after being converged through the flue gas tail gas converging cavity 4.
The invention is in modularized design, and the modules are quickly disassembled and assembled through the V-shaped clamp 11 or the clamp sleeve. Wherein, a plurality of the methanol water evaporators 6 are connected through an annular bracket, and are circumferentially and uniformly distributed on the outer surface of the reforming reactor 5, so that the reforming reaction pipes are ensured to correspond to the vaporizing cavity flow passages 20 one by one. The flue gas side inlet and the evaporation side outlet of the reforming reactor 5 are detachably connected through flange surfaces and bolts, and metal graphite composite gaskets are filled in the connecting surfaces. The evaporation side inlet of the reforming reactor 5 is detachably connected with the flow equalizing ring 7 by using a stainless steel clamping sleeve, and the flue gas side outlet is detachably connected with the flue gas tail gas converging cavity 4 by using a stainless steel clamping sleeve.
According to the invention, temperature sensors are respectively arranged at the outlet of the oxidation reactor 3, the outlet of the flue gas side of the reformer, the outlet of the evaporation side of the evaporator, the outlet of the flue gas tail gas converging cavity 4, the outlet F of the reforming side of the reformer and the reforming reaction tube 14 of the reformer, and pressure sensors are arranged on the converging module 8 of the outlet of the reforming side, so that the monitoring and control of each link of the whole reformer system are realized, and meanwhile, the basis is provided for automatic control.
In one embodiment, the base temperature of each reforming reaction flow path in the reforming reactor 5 is determined by the recorded data of the temperature sensor during test run of the sample machine before grouping, or the temperature data obtained in digital simulation, and the reforming reaction flow paths with the base temperature difference within 25 ℃ are grouped into one group, and at least three reforming reaction flow paths are included in one group. After grouping, the reforming reaction groups are in one-to-one correspondence with the evaporation groups, and the input flow of the evaporation cavity flow channels 20 in the evaporation groups is set, and each evaporation cavity flow channel 20 in each evaporation group is controlled to input methanol water with the same flow rate through the same flow equalizing ring 7. On the basis of the grouping, compared with a group of reforming reaction groups with lower average basic temperature, the group of reforming reaction groups with higher average basic temperature is controlled to have larger flow rate of methanol input through the evaporation group, so that the flow rate of each evaporation cavity flow channel 20 is controlled, the problem of uneven liquid inlet of each reaction tube at the reforming side of the reformer is solved, and the overall heat efficiency of the system is effectively improved.
In addition, the flow equalizing plates 18 and the baffle plates 19 with alternating sizes are arranged on the shell side in the flow direction, and the number of the flow equalizing plates 18 and the baffle plates 19 arranged in the reforming reaction group with high average base temperature is more than that in the reforming reaction group with low average base temperature, so that the reaction efficiency in the reforming reaction group with high average base temperature can be further improved. The flow equalization plates 18 enable hot flue gas to be evenly distributed on the section of the shell side of the reformer, the baffle plates 19 enable the hot flue gas entering the shell side to increase the flow path length, the heat transfer time of the hot flue gas and the reaction tubes to increase the effective heat transfer, the flow equalization plates 18 and the baffle plates 19 are distributed according to the designed interval, the reforming reaction tubes are seamless steel tubes, and the diameter range is 12-30 mm. The wall thickness is 1-2 mm, and the material is 304, 316 or 310s stainless steel.
As shown in fig. 7, the flow equalizing plate 18 is a first plate located in the flue gas side flow channel of the reforming reactor, and is located before the first baffle plate 19, wherein the large holes are connecting holes connected with the reforming reaction tubes 14, and are in a plugging state after connection, small holes are formed in the flow equalizing plate 18, and the size and arrangement mode of the small holes are calculated according to requirements. The flow equalizing plate 18 has the main functions of: 1. increasing the residence time of the hot flue gas in the area, and further heating the methanol vapor in the connecting pipe of the evaporator and the reforming reaction pipe; 2. ensuring that each reaction tube on the section is heated uniformly after passing through the flow equalizing plate 18.
Specifically, in the cold start stage, an air inlet B is connected with an air compressor and is filled with a certain amount of air, electric heating is started in an oxidation reactor 3, after the air passes through the electric heating area, heat is transferred to a rear section metal honeycomb structure through the air, so that the oxidation catalyst is quickly heated to an active temperature range, at the moment, a methanol aqueous solution is sprayed into an air inlet liquid inlet mixing end cover 2 through a methanol atomizing nozzle 1 to be fully mixed with the air and enter the oxidation reactor 3 along with the air to perform catalytic oxidation reaction to release a large amount of heat, the heat is transferred backwards along with mixed gas, the liquid inlet amount and the air inlet amount are adjusted according to a set air-fuel ratio range, and the heat release power of the oxidation reactor 3 is gradually improved; the high-temperature mixed flue gas sequentially enters a shell side flow passage of the reformer and a flue gas side flow passage of the evaporator, and the reformer and the evaporator are gradually preheated; when the outlet temperature of the flue gas side of the evaporator reaches a certain value, a small amount of methanol aqueous solution is introduced into the evaporator through the flow equalizing ring 7 by the liquid inlet system, the part of methanol aqueous solution flows into the reaction tube at the tube side of the reformer after being evaporated by the evaporator, and gradually absorbs heat and heats up in the flowing process, so that the temperature of the rear section in the reforming reaction tube is rapidly increased, the whole temperature of the reaction tube is rapidly increased to an active temperature range, and the system enters a low-power steady state at the moment; according to the law of power switching, the liquid inlet amount and the air inlet amount of the oxidation reactor 3 and the liquid inlet amount of the methanol water at the side of the evaporator are regulated in sequence according to the control parameters of each steady state with a set power span, and the regulation is gradually carried out from a low-power steady state to a high-power steady state; in the steady state of each power section, the temperature interval of the outlet of the oxidation side is controlled to be 550-650 ℃, the controllable range of the temperature interval in the reaction tube of the reformer is 200-550 ℃, the temperature range of the outlet D of the tail gas is 60-100 ℃, the temperature interval of the outlet F of the reforming side is 200-550 ℃, and the pressure interval of the reforming side of the reformer is 2-5bar.
Claims (8)
1. The modularized methanol reforming hydrogen production device comprises a reforming reactor with a plurality of reforming reaction pipes inside, wherein a reforming reaction flow passage positioned in the reforming reaction pipes is a pipe side, a main heat supply flow passage positioned outside the pipe is a shell side, the modularized methanol reforming hydrogen production device is characterized in that the front end of the shell side of the reforming reactor is communicated with an oxidation reactor, the front end of the oxidation reactor is provided with an air inlet and liquid inlet mixed end cover, the air inlet and liquid inlet mixed end cover is provided with an oxidation side methanol water inlet and an air inlet,
Each reforming reaction tube is respectively connected with a methanol water evaporator,
The reforming reactor comprises a plurality of reforming reaction groups and a corresponding number of evaporation groups, wherein each reforming reaction group comprises a plurality of reforming reaction channels with similar basic temperature in the channels, the reforming reaction groups are in one-to-one correspondence with the evaporation groups, the evaporation groups corresponding to the reforming reaction groups comprise a plurality of methanol water evaporators for gasifying methanol water and inputting the gasified methanol water into the reforming reaction channels,
The methanol-water evaporator is connected with the reforming side methanol-water inlet through a flow equalizing ring, a plurality of split rings are concentrically arranged in the flow equalizing ring, the flow channels in the split rings are used as pressure stabilizing cavities, each pressure stabilizing cavity is respectively connected with an inlet pipe and a plurality of outlet pipes respectively connected with the methanol-water evaporator, the inlet pipes are connected with the reforming side methanol-water inlet provided with a liquid inlet system, and the cross section area of each inlet pipe is larger than the total cross section area of each outlet pipe.
2. A modular methanol reforming hydrogen generator as in claim 1 wherein the oxidation side methanol water inlet is provided with a methanol atomizing nozzle.
3. The modular methanol reforming hydrogen generator as in claim 1 wherein each methanol water evaporator comprises a vaporization cavity flow channel and an auxiliary heat supply flow channel closely attached to the vaporization cavity flow channel, the vaporization cavity flow channels and the corresponding auxiliary heat supply flow channels are divided into a plurality of vaporization groups, the reforming reaction groups are in one-to-one correspondence with the vaporization groups, the front end of each auxiliary heat supply flow channel is respectively communicated with the tail end of one main heat supply flow channel, the tail end of each vaporization cavity flow channel is respectively communicated with the front end of one reforming reaction tube, and the vaporization cavity flow channels of each vaporization group are respectively connected with the methanol water inlet on the reforming side through flow equalizing rings.
4. A modular methanol reforming hydrogen generator as in claim 1 wherein the oxidation reactor is honeycomb in cross section, wherein an oxidation catalyst is coated in the oxidation reactor, and wherein the front section of the oxidation reactor is an electric heating device of iron-chromium-aluminum material.
5. A modular methanol reforming hydrogen generator as in claim 1 wherein a segmented microchannel support is provided within the reforming reaction tube, the segmented microchannel support being coated with a methanol reforming hydrogen catalyst.
6. A modular methanol reforming hydrogen generator as in claim 1 wherein the tube side end is connected to an outlet manifold module having a pressure regulating device disposed therein.
7. A modular methanol reforming hydrogen generator as in claim 1 wherein the shell side has flow equalization plates and baffles of alternating size in the direction of flow, the number of equalization plates and baffles in the reforming reaction set having a higher average base temperature being greater than the number of baffles in the reforming reaction set having a lower average base temperature.
8. A modular methanol reforming hydrogen generator as in claim 1 wherein said methanol water vaporizers are circumferentially distributed about the outer surface of said reforming reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410513770.XA CN118083911A (en) | 2024-04-26 | 2024-04-26 | Modularized methanol reforming hydrogen production device |
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0206608A2 (en) * | 1985-06-10 | 1986-12-30 | United States Department Of Energy | Fuel cell integrated with steam reformer |
| US5939025A (en) * | 1995-08-23 | 1999-08-17 | The University Of Chicago | Methanol partial oxidation reformer |
| KR20040085623A (en) * | 2003-04-01 | 2004-10-08 | 김동현 | Methanol autothermal reformer for hydrogen production |
| CN109761193A (en) * | 2019-03-20 | 2019-05-17 | 浙江工业大学 | A kind of preparing hydrogen by reforming methanol reactor |
| CN111617728A (en) * | 2020-06-29 | 2020-09-04 | 上海博氢新能源科技有限公司 | Heat exchange type reforming reactor and reforming hydrogen production system |
| CN111617727A (en) * | 2020-06-29 | 2020-09-04 | 上海博氢新能源科技有限公司 | Electrical heating type reforming reactor and reforming hydrogen production system |
| CN111762757A (en) * | 2020-06-28 | 2020-10-13 | 上海齐耀动力技术有限公司 | Heating system and method for hydrogen production by methanol reforming |
| CN212492959U (en) * | 2020-06-29 | 2021-02-09 | 上海博氢新能源科技有限公司 | Heat exchange type reforming reactor and reforming hydrogen production system |
| CN114436210A (en) * | 2022-03-07 | 2022-05-06 | 广东工业大学 | High-efficient integrated distributed methanol reforming hydrogen production purification system |
| CN115159454A (en) * | 2022-06-30 | 2022-10-11 | 苏州氢洁电源科技有限公司 | Methanol reforming reactor with internal integrated evaporator |
-
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- 2024-04-26 CN CN202410513770.XA patent/CN118083911A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0206608A2 (en) * | 1985-06-10 | 1986-12-30 | United States Department Of Energy | Fuel cell integrated with steam reformer |
| US5939025A (en) * | 1995-08-23 | 1999-08-17 | The University Of Chicago | Methanol partial oxidation reformer |
| KR20040085623A (en) * | 2003-04-01 | 2004-10-08 | 김동현 | Methanol autothermal reformer for hydrogen production |
| CN109761193A (en) * | 2019-03-20 | 2019-05-17 | 浙江工业大学 | A kind of preparing hydrogen by reforming methanol reactor |
| CN111762757A (en) * | 2020-06-28 | 2020-10-13 | 上海齐耀动力技术有限公司 | Heating system and method for hydrogen production by methanol reforming |
| CN111617728A (en) * | 2020-06-29 | 2020-09-04 | 上海博氢新能源科技有限公司 | Heat exchange type reforming reactor and reforming hydrogen production system |
| CN111617727A (en) * | 2020-06-29 | 2020-09-04 | 上海博氢新能源科技有限公司 | Electrical heating type reforming reactor and reforming hydrogen production system |
| CN212492959U (en) * | 2020-06-29 | 2021-02-09 | 上海博氢新能源科技有限公司 | Heat exchange type reforming reactor and reforming hydrogen production system |
| CN114436210A (en) * | 2022-03-07 | 2022-05-06 | 广东工业大学 | High-efficient integrated distributed methanol reforming hydrogen production purification system |
| CN115159454A (en) * | 2022-06-30 | 2022-10-11 | 苏州氢洁电源科技有限公司 | Methanol reforming reactor with internal integrated evaporator |
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