CN111661818B - An integrated hydrocarbon autothermal reforming reactor for hydrogen production - Google Patents
An integrated hydrocarbon autothermal reforming reactor for hydrogen production Download PDFInfo
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- CN111661818B CN111661818B CN202010413922.0A CN202010413922A CN111661818B CN 111661818 B CN111661818 B CN 111661818B CN 202010413922 A CN202010413922 A CN 202010413922A CN 111661818 B CN111661818 B CN 111661818B
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1288—Evaporation of one or more of the different feed components
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Abstract
The invention discloses an integrated hydrocarbon autothermal reforming hydrogen production reactor, which comprises an evaporation unit, a catalytic reaction unit, a mixing and heat exchange unit and a liquid-gas separation unit which are sequentially connected, wherein the evaporation unit comprises an air inlet pipe, a heating rod, a thermocouple and an evaporation body, and the evaporation unit ensures normal vaporization of fuel; the catalytic reaction unit comprises a reaction cylinder, a catalyst carrier, a heating ring and a thermocouple, and ensures the normal operation of the catalytic reaction of the fuel; a reaction product flow channel and a liquid fuel mixing closed space are arranged in the mixing and heat exchange unit, so that the mixing and preheating of the fuel are realized; the liquid-gas separation unit is internally provided with a liquid collecting cavity and a liquid discharging hole for separating liquid and gaseous reaction products. The invention has the characteristics of integrating the functions of mixing, evaporating, catalytic reaction, heat exchange and liquid-gas separation, and has the advantage of improving the heat utilization rate of a reaction system.
Description
Technical Field
The invention relates to the field of fuel cells, in particular to an integrated hydrocarbon autothermal reforming hydrogen production reactor.
Background
The fuel cell is used as a power generation device for directly converting chemical energy into electric energy, and has the characteristics of high energy conversion efficiency, zero emission, low noise and the like. The proton exchange membrane fuel cell has the advantages of low working temperature, quick starting, high working current, large specific power energy density, no corrosion, zero noise, zero pollution, long service life and the like, and becomes the optimal choice of the mobile power supply.
At present, a direct hydrogen storage mode is generally adopted for the fuel cell, but the direct hydrogen storage has the problems of low energy density, huge volume, storage and transportation dangers and the like, and severely limits the development of the fuel cell. In-situ hydrogen production is considered to be one of the ways in which the problem of direct hydrogen storage can be effectively solved, namely, hydrogen is generated on site through a reaction system by adopting liquid hydrocarbon with high energy density to be supplied to a fuel cell. At present, the hydrogen production method presents various patterns, and the preparation of hydrogen by reforming hydrocarbon is a research hot spot in the field.
Typical hydrocarbon reforming reaction hydrogen production can be divided into three types: steam reforming, partial oxidation reforming and autothermal reforming,
Although the steam reforming method can produce hydrogen with a relatively high purity, this reaction is endothermic, requires an external heat source, and has low thermal efficiency. The partial oxidation reforming process is an exothermic reaction that can be performed at a lower temperature, but the purity of hydrogen is relatively low. The autothermal reforming method combines steam reforming and partial oxidation reforming, and can obtain high-purity hydrogen without external heat supply after the reaction is started, so the autothermal reforming reaction hydrogen production is a research hot spot.
Because the autothermal reforming reaction of hydrocarbon includes processes such as mixing, evaporation, catalytic reaction, heat exchange, liquid-gas separation, etc., most reforming hydrogen production reactors are independent of each other, resulting in huge whole reaction system and serious heat loss during the reaction. Aiming at the problem, the invention provides the hydrocarbon autothermal reforming hydrogen production reactor integrating the functions of mixing, evaporating, catalytic reaction, heat exchange and liquid-gas separation, which has compact structure and improves the heat utilization rate of a reaction system.
Disclosure of Invention
In order to overcome the defects and shortcomings in the prior art, the invention provides an integrated hydrocarbon autothermal reforming hydrogen production reactor, which integrates the functions of mixing, evaporation, catalytic reaction, heat exchange and liquid-gas separation.
The invention adopts the following technical scheme:
An integrated hydrocarbon autothermal reforming hydrogen production reactor comprises an evaporation unit, a catalytic reaction unit, a mixing and heat exchange unit and a liquid-gas separation unit which are connected in sequence, wherein:
The evaporation unit comprises an air inlet pipe, a heating rod and an evaporation body, wherein the heating rod is arranged in the evaporation body, the evaporation body is provided with a preheated liquid fuel inlet, an air and preheated fuel mixing channel and a mixed gaseous fuel outlet, two ends of the evaporation body are provided with fuel evaporation micro-channels, and the preheated liquid fuel inlet, the fuel evaporation micro-channels, the air and preheated fuel mixing channel and the mixed gaseous fuel outlet are sequentially communicated to form a fuel mixed evaporation flow channel;
the catalytic reaction unit comprises a reaction cylinder, a catalyst carrier and a heating ring, wherein a reaction cavity is arranged in the reaction cylinder, the heating ring is arranged on the outer side of the reaction cavity, the catalyst carrier is arranged at the bottom of the reaction cavity, a preheated liquid fuel conveying channel is arranged on one side of the reaction cylinder and is communicated with a preheated liquid fuel inlet, a mixed gaseous fuel inlet is arranged at the top of the reaction cylinder and is communicated with a mixed gaseous fuel outlet of the evaporation unit, and a reaction cylinder lower plate provided with a high-temperature reaction product outlet is arranged at the bottom of the reaction cylinder;
The mixing and heat exchanging unit comprises a heat exchanging sleeve, two ends of the heat exchanging sleeve are provided with a heat exchanging upper plate and a heat exchanging lower plate, a reaction product flow channel formed by a plurality of guide pipes is arranged in the heat exchanging sleeve, the heat exchanging upper plate is provided with a mixed liquid fuel outlet and an inlet of the reaction product flow channel, the inlet of the reaction product flow channel is communicated with a high-temperature reaction product outlet of the catalytic reaction unit, the mixed liquid fuel outlet is communicated with a preheated liquid fuel transportation channel of the catalytic reaction unit, the heat exchanging lower plate is provided with a reaction product flow channel outlet, two sides of the heat exchanging sleeve are provided with a hydrocarbon inlet and a water inlet, and a space between the heat exchanging sleeve and the guide pipes forms a mixing space of hydrocarbon and water;
The liquid-gas separation unit comprises a cooling reaction product outlet, a liquid collecting cavity and an outer cavity, wherein the liquid collecting cavity and the outer cavity are respectively communicated with a reaction product circulation channel corresponding to the mixing and heat exchange unit, the liquid collecting cavity is provided with a liquid discharging hole for separated liquid products to flow out, and the cooling reaction product outlet is communicated with the outer cavity.
Thermocouples are arranged in the evaporation body and the reaction cylinder.
The upper end of the evaporation body is provided with an evaporation upper plate, an evaporation body upper gasket is arranged between the evaporation upper plate and the evaporation body for sealing, an evaporation body lower gasket is arranged between the evaporation body and the catalytic reaction unit for sealing, and the mixed gaseous fuel outlet is arranged at the central position of the evaporation body lower gasket.
The fuel vaporization microchannel includes an annular microchannel and a straight microchannel.
The mixed gaseous fuel inlet and the high temperature reaction product outlet have a tapered opening.
The reaction product flow channel is composed of flow guide pipes which are arranged outwards from the center of the heat exchange sleeve, the flow guide pipes are vertically arranged, the flow guide pipe positioned at the center of the heat exchange sleeve is one, the top of the flow guide pipe is communicated with the inlet of the reaction product flow channel, other flow guide pipes are symmetrically arranged towards two sides by taking the flow guide pipe positioned at the center of the heat exchange sleeve as the flow guide pipe, the flow guide pipes are communicated with each other in a head-tail mode, and the last group of flow guide pipes are communicated with the outlet of the reaction product flow channel.
The heat exchange upper plate is provided with an annular groove, and the heat exchange lower plate is provided with a circular groove.
The evaporation unit, the catalytic reaction unit, the mixing and heat exchange unit and the liquid-gas separation unit are all provided with flange structures.
Preferably, the honeycomb duct is divided into three groups, sets up the honeycomb duct in center and is first group, outwards is second group and third group respectively along center one side, the lower extreme of first group communicates with the lower extreme of second group through the circular recess of heat transfer hypoplastron, the upper end of second group communicates with the third group upper end through the annular recess of heat transfer upper plate.
Preferably, the liquid collecting cavity is communicated with the lower ends of the first group of flow guiding pipes and the second group of flow guiding pipes, and the outer cavity is communicated with the lower ends of the third group of flow guiding pipes.
The working process of the invention is as follows: the liquid hydrocarbon fuel a and the water B in the mixing and heat exchanging unit are mixed in the mixing and heat exchanging unit, and further the mixed liquid fuels a and B are preheated by heat exchanging with the gaseous reaction product D, the preheated mixed liquid fuels a and B flow into the evaporating unit, the heating rod heats to vaporize the preheated mixed liquid fuels a and B and mix with the air C, and the resultant mixed gaseous fuels A, B and C finally flow into the catalytic reaction unit; the heating ring heats the catalytic reaction unit to a preset reaction temperature, at this time, mixed gaseous fuel A, B and C in the catalytic reaction unit generate autothermal reforming hydrogen production reaction under the combined action of temperature and catalyst to generate hydrogen and a small amount of byproducts, and when the autothermal reforming reaction is carried out, the heating of the heating ring is stopped, and the obtained gaseous reaction product D flows into the mixing and heat exchange unit;
the gaseous reaction product D in the mixing and heat exchanging unit exchanges heat with the mixed liquid fuels A and B, the gaseous reaction product D after heat exchanging flows into the liquid-gas separation unit, part of the reaction product is liquefied after being cooled and flows into a liquid collecting cavity of the liquid-gas separation unit, and the gaseous reaction product D finally passes through an outer cavity of the liquid-gas separation unit and is finally discharged through a cooling reaction product outlet.
The invention has the beneficial effects that:
(1) The hydrogen produced by the autothermal reforming method has the advantages of high purity and less impurities, is used on site, does not reach the explosion limit, has better safety, and solves the problem of hydrogen storage.
(2) The invention recovers the residual heat of the reaction product to preheat the fuel, heats the liquid fuel, cools the reaction product, and improves the heat utilization rate of the reaction system.
(3) The whole autothermal reforming hydrogen production reactor has compact volume, integrates the functions of mixing, evaporating, catalytic reaction, heat exchange and liquid-gas separation, can increase or reduce the number of units according to the needs, and can adapt to scale expansion and shrinkage.
Drawings
FIG. 1 is a schematic diagram of an integrated hydrocarbon autothermal reforming reactor in accordance with the present invention;
FIG. 2 is a schematic diagram of a mixing and heat exchange unit in accordance with an embodiment of the present invention;
FIG. 3 is a top view of a heat exchange upper plate of a hybrid and heat exchange unit in accordance with an embodiment of the present invention;
FIG. 4 is a bottom view of a lower plate of a hybrid and heat exchanger unit in accordance with an embodiment of the present invention;
FIG. 5 is a schematic view showing the structure of an evaporation unit according to an embodiment of the present invention;
FIG. 6 is a top view of an evaporator body of an evaporation unit in an embodiment of the invention;
FIG. 7 is a bottom view of an evaporator body of an evaporation cell in an embodiment of the invention;
FIG. 8 is a schematic diagram of a catalytic reaction unit in an embodiment of the invention;
FIG. 9 is a top view of a cartridge of a catalytic reaction unit in an embodiment of the invention;
fig. 10 is a top view of a liquid-gas separation unit in an embodiment of the invention.
Detailed Description
The present invention will be described in further detail with reference to examples and drawings, but embodiments of the present invention are not limited thereto.
Examples
Referring to fig. 1, an integrated hydrocarbon autothermal reforming reactor integrates mixing, evaporating, catalytic reaction, heat exchange and liquid-gas separation functions, and mainly comprises an evaporating unit 1, a catalytic reaction unit 2, a mixing and heat exchange unit 3 and a liquid-gas separation unit 4 which are connected in sequence.
Referring to fig. 1, 5, 6 and 7, the evaporation unit 1 includes an air inlet pipe 11, a thermocouple junction pipe 12, a thermocouple junction long pipe 13, a heating rod 18, an evaporation upper plate 14, an evaporation body upper gasket 16, an evaporation body 15 and an evaporation body lower gasket 17. The evaporation upper plate 14 and the evaporation body 15 are all in flange structures, and through holes 106 for connecting bolts are arranged on the periphery of the evaporation upper plate and are used for being connected with the catalytic reaction unit 2. An upper evaporator spacer 16 is placed between the upper evaporator plate 14 and the evaporator 15 for sealing, and a lower evaporator spacer 17 is placed between the evaporator 15 and the catalytic reaction unit 2 for sealing. The center of the lower evaporator shim 17 is provided with a mixed gaseous fuel outlet 102. The fuel evaporation micro-channels are arranged at the two ends of the evaporation body and comprise annular micro-channels and straight micro-channels. The evaporation body 15 is provided with a preheated liquid fuel inlet 101, an air and preheated fuel mixing channel 103 and a catalytic reaction temperature measuring hole 109, the preheated liquid fuel inlet 101 is communicated with the annular micro-channel 104 through an inlet groove 107, the other end of the annular micro-channel 104 is communicated with the air and preheated fuel mixing channel 103 through an outlet groove 108, and the lower end of the air and preheated fuel mixing channel 103 is communicated with the straight micro-channel 105. The air inlet pipe 11, the evaporating body 15, the upper evaporating body gasket 16 and the lower evaporating body gasket 17 form an evaporating passage of the mixed fuel. The thermocouple junction pipe 12 is welded and fixed with the evaporation upper plate 14, and the temperature of the evaporation body 15 can be monitored and controlled after the short thermocouple is inserted; the thermocouple is connected with the long tube 13 and welded with the evaporation upper plate 14, and the long thermocouple is inserted and then extends into the reaction cavity 201 of the catalytic reaction unit 2 through the catalytic reaction temperature measuring hole 109, so that the temperature of the catalytic reaction unit 2 can be monitored and controlled.
The working process of the evaporation unit is as follows: the mixed liquid fuels A and B preheated by the mixing and heat exchanging unit 3 enter through the preheated liquid fuel inlet 101, flow into the annular micro-channel 104 through the inlet groove 107, preheat the mixed liquid fuels A and B under the heating action of the heating rod 18, vaporize the mixed liquid fuels A and B into gaseous fuels A and B, and flow into the air and preheated fuel mixing channel 103 through the outlet groove 108; at the same time, air C flows into the air-preheated fuel mixing channel 103 through the air inlet pipe 11, is mixed with the gaseous fuels a and B to form mixed gaseous fuels A, B and C, and then flows out from the mixed gaseous fuel outlet 102 of the evaporator lower gasket 17 through the straight micro-channel 105, and the flow paths of the mixed liquid fuels a and B in the evaporation unit 1 are d→e→f.
Referring to fig. 1, 8 and 9, the catalytic reaction unit 2 includes a reaction cylinder 21, a catalyst carrier 22, a reaction cylinder lower plate 23 and a heating ring 24, where the reaction cylinder 21 and the reaction cylinder lower plate 23 both adopt a flange structure, through holes 205 for connecting bolts are uniformly distributed along the circumference and are used for connection with the evaporation unit 1 and the mixing and heat exchange unit 3, and gaskets are placed between the reaction cylinder 21 and the reaction cylinder lower plate 23 for sealing and fixedly connected by bolts. The reaction cylinder 21 is provided with a preheated liquid fuel transportation channel 202; the reaction cylinder 21 has an inner space of a reaction cavity 201, a heating ring 24 is installed on the outer side of the reaction cavity 201, a catalyst carrier 22 is installed at the bottom in the reaction cavity 201, a mixed gaseous fuel inlet 203 is arranged at the top of the reaction cavity 201, and the mixed gaseous fuel inlet 203 has a conical part with a downward opening, so that mixed gaseous fuel A, B and C can be quickly dispersed when flowing in and uniformly flow through the catalyst carrier 22. A long thermocouple extends into the reaction chamber 201 through the mixed gaseous fuel inlet 203 to monitor and control the temperature of the catalytic reaction unit 2. The reaction cylinder lower plate 23 is provided with a preheated liquid fuel transporting channel 202 and a high-temperature reaction product outlet 204, and the high-temperature reaction product outlet 204 is provided with a conical part with an upward opening, so that gaseous reaction products D obtained by the autothermal reforming reaction can be quickly collected and flow out.
Referring to fig. 8 and 9, the catalytic reaction unit 2 operates as follows: the heating ring 24 preheats the temperature in the reaction chamber 201 to a set reaction temperature in advance, then the mixed gaseous fuels A, B and C enter the reaction chamber 201 from the mixed gaseous fuel inlet 203, under the combined action of the temperature and the catalyst, the mixed gaseous fuels A, B and C undergo an autothermal reforming reaction to produce hydrogen and a small amount of by-products, the heating of the heating ring 24 is stopped when the autothermal reforming reaction proceeds, and the obtained gaseous reaction product D flows out through the high-temperature reaction product outlet 204. On the other hand, the mixed liquid fuels a and B flow through the preheated liquid fuel transporting passage 202 of the catalytic reaction unit 2.
Referring to fig. 1, 2, 3 and 4, the mixing and heat exchange unit 3 includes a heat exchange upper plate 31, a heat exchange sleeve 32, a heat exchange lower plate 34 and a draft tube 33. Wherein, the heat exchange upper plate 31 is provided with a mixed liquid fuel outlet 303; the heat exchange upper plate 31 and the heat exchange lower plate 34 adopt flange structures, and through holes 306 for connecting bolts are uniformly distributed around the heat exchange upper plate and the heat exchange lower plate and are respectively used for being connected with the catalytic reaction unit 2 and the liquid-gas separation unit 4. The heat exchange sleeve 32 is provided with a reaction product flow channel 304 formed by connecting a plurality of flow guide pipes 33, and is used for flowing gaseous reaction products D. The mixing enclosure 302 between the heat exchange sleeve 32 and the draft tube 33 is used for mixing the hydrocarbon liquid fuel a and water B. The two sides of the heat exchange sleeve 32 are provided with a liquid hydrocarbon inlet 301 and a water inlet 307, and the two inlets are distributed at 180 degrees.
Referring to fig. 2, 3 and 4, in the mixing and heat exchange unit 3, the reaction product flow channel 304 is formed of three groups of vertical draft tubes arranged outwardly from the center of the heat exchange sleeve 32, a first group, a second group and a third group, respectively, outwardly from the center, wherein one group at the center includes one draft tube, the other groups include a plurality of draft tubes 33 uniformly arranged in the circumferential direction, and the diameter of the draft tube near the center is larger than that of the draft tube near the outer side. The multiple groups of flow guiding pipes 33 are sequentially communicated end to end along the up-down direction to form a reaction product flow channel 304, so that the gaseous reaction product D can flow back and forth in the vertical direction, the flow path is prolonged, and full heat exchange is realized. Specifically, a through hole for installing the flow guide pipe 33 is arranged in the center of the heat exchange upper plate 31, and the end part of the corresponding flow guide pipe 33 is inserted into the through hole and welded and fixed; the upper surface of the heat exchange upper plate 31 is provided with an annular groove 3101, the bottom of the annular groove 3101 is provided with a plurality of through holes for installing the flow guide pipes 33, and the end parts of the corresponding flow guide pipes 33 are inserted into the through holes and welded and fixed. The center of the lower surface of the heat exchange lower plate 34 is provided with a circular groove 3401, the bottom of the circular groove 3401 is provided with a plurality of through holes for installing the flow guide pipes 33, and the end parts of the corresponding flow guide pipes 33 are inserted into the through holes and welded and fixed; the circular groove 3401 of the heat exchange lower plate 34 is provided with a plurality of through holes for installing the flow guide pipes 33 at one turn, and the ends of the corresponding flow guide pipes 33 are inserted into the through holes and welded and fixed. The upper ends of the first group of flow guiding pipes form a reaction product flow channel inlet 305, the lower ends of the first group of flow guiding pipes are communicated with the lower ends of the second group of flow guiding pipes through circular grooves 3401 on the heat exchange lower plate 34, the upper ends of the second group of flow guiding pipes are communicated with the upper ends of the third group of flow guiding pipes through annular grooves 3101 on the heat exchange upper plate 31, and the lower ends of the third group of flow guiding pipes form a reaction product flow channel outlet 308, so that the reaction product flow channel 304 is formed.
Referring to fig. 2,3 and 4, the above-mentioned mixing and heat exchange unit 3 operates as follows: on the one hand, the mixed gaseous reaction product D such as hydrogen obtained by the autothermal reforming reaction of the catalytic reaction unit 2 enters through the reaction product flow channel inlet 305 of the heat exchange upper plate 31, flows into the circular groove 3401 in the center of the heat exchange lower plate 34 through the first group of flow guide pipes, flows back to the annular groove 3101 of the heat exchange upper plate through the second group of flow guide pipes, finally flows to the heat exchange lower plate 34 through the third group of flow guide pipes and flows out, and the flow path of the gaseous reaction product D in the mixed and heat exchange unit 3 is g- > h- > i- > j; at the same time, the hydrocarbon liquid fuel a and the water B enter the mixing enclosed space 302 from the liquid hydrocarbon inlet 301 and the water inlet 307 of the heat exchange sleeve 32 respectively for mixing, and as the flow guide pipe 33 is soaked in the mixed liquid fuels a and B, the heat of the high-temperature reformed gas flowing through the flow guide pipe 33 is transferred to the mixed liquid fuels a and B with lower temperature for preheating, preparation is made for the vaporization of the mixed liquid fuels a and B in the evaporation unit 1, finally the preheated mixed liquid fuels a and B flow out from the mixed liquid fuel outlet 303, and the flow paths of the hydrocarbon liquid fuels a and the water B in the mixing and heat exchange unit 3 are a1, a 2- & gtb- & gtc.
Referring to fig. 10, the liquid-gas separation unit 4 is provided in a flange structure, and through holes 405 for connecting bolts with the mixing and heat exchange unit 3 are provided around. The liquid-gas separation unit 4 is provided with a liquid collecting cavity 402 and an outer cavity 403, and the liquid collecting cavity 402 is provided with a liquid discharging hole 404 for the separated liquid product to flow out; the side of the liquid-gas separation unit 4 is provided with a cooling reaction product outlet 401 which is communicated with an outer cavity 403.
Referring to fig. 1-10, in the hydrocarbon autothermal reforming hydrogen production reactor integrating the functions of mixing, evaporating, catalytic reaction, heat exchange and liquid-gas separation, the air inlet pipe 11 is communicated with the air and preheated fuel mixing channel 103 of the evaporating unit 1; the mixing closed space 302 of the mixing and heat exchange unit 3 is sequentially communicated with the preheated liquid fuel transportation channel 202 of the catalytic reaction unit 2, the preheated liquid fuel inlet 101 of the evaporation unit 1, the reaction chamber 201 of the catalytic reaction unit 2, the reaction product flow channel 304 of the mixing and heat exchange unit 3, the liquid collecting chamber 402 and the outer chamber 403 of the liquid-gas separation unit 4, and specifically, the overlapping relationship and alignment manner of the units are as follows:
The evaporation unit 1 is arranged above the catalytic reaction unit 2, and a preheated liquid fuel inlet 101 of the evaporation unit 1 is communicated with a preheated liquid fuel transportation channel 202 of the catalytic reaction unit 2 in an aligned manner; the mixed gaseous fuel outlet 102 of the vaporization unit 1 is in aligned communication with the mixed gaseous fuel inlet 203 of the catalytic reaction unit 2; the plurality of through holes 106 for the connecting screw thread on the evaporation unit 1 are respectively aligned and communicated with the through holes 205 for the connecting screw thread of the catalytic reaction unit 2, and the two units (not shown) are locked by bolts.
The catalytic reaction unit 2 is arranged between the evaporation unit 1 and the mixing and heat exchange unit 3, and the preheated liquid fuel transportation channel 202 of the catalytic reaction unit 2 is communicated with the mixed liquid fuel outlet 303 of the mixing and heat exchange unit 3 in an aligned manner; the high temperature reaction product outlet 204 of the catalytic reaction unit 2 is in aligned communication with the reaction product flow channel inlet 305 of the mixing and heat exchange unit 3; the through holes 205 for the plurality of connecting threads of the catalytic reaction unit 2 are respectively aligned and communicated with the through holes 306 for the plurality of connecting threads of the mixing and heat exchange unit 3, and the two units are locked by bolts, and a graphite gasket seal (not shown) is arranged between the two units.
The mixing and heat exchange unit 3 is installed between the catalytic reaction unit 2 and the liquid-gas separation unit 4, the liquid hydrocarbon inlet 301 of the mixing and heat exchange unit 3 is aligned with the cooling reaction product outlet 401 of the liquid-gas separation unit 4 on the same side, the through holes 306 for the plurality of connecting threads of the mixing and heat exchange unit 3 are respectively aligned with the through holes 405 for the plurality of connecting threads of the liquid-gas separation unit 4 for locking the two units by connecting bolts, and a graphite gasket seal (not shown) is placed between the two units.
Referring to fig. 1-10, the hydrocarbon autothermal reforming hydrogen production reactor integrating mixing, evaporation, catalytic reaction, heat exchange, and liquid-gas separation functions operates as follows:
In practice, hydrocarbon liquid fuel a and water B enter from liquid hydrocarbon inlet 301 and water inlet 307, respectively, of mixing and heat exchange unit 3 and are mixed in mixing enclosure 302; the diversion pipe of the mixing and heat exchange unit 3 is soaked in the mixed liquid fuels A and B, so that the heat of the gaseous reaction product D in the diversion pipe of the mixing and heat exchange unit 3 is transferred to the mixed liquid fuels A and B with lower temperature; the preheated mixed liquid fuels A and B flow through the preheated liquid fuel transportation channel 202 of the catalytic reaction unit 2 from the mixed liquid fuel outlet 303 of the mixing and heat exchange unit 3, enter through the preheated liquid fuel inlet 101 of the evaporation unit 1, are vaporized in the annular micro-channel 104 under the heating action of the heating rod 18, are fully mixed with air C in the air and preheated fuel mixing channel 103, and enter the reaction cavity 201 through the mixed gaseous fuel inlet 203 of the catalytic reaction unit 2 after the mixed gaseous fuels A, B and C flow out through the mixed gaseous fuel outlet 102, and generate hydrogen and a small amount of byproducts under the combined action of the heating ring 24 and the catalyst carrier 22, and the heat supply of the heating ring 24 is stopped when the autothermal reforming reaction is performed; the high-temperature gaseous reaction product D flows into the reaction product flow channel inlet 305 of the mixing and heat exchange unit 3 through the high-temperature reaction product outlet 204 of the catalytic reaction unit 2; the gas after being split flows into the heat exchange upper plate 31 through the second group of flow guiding pipes after being split flows into the outer cavity 403 of the liquid-gas separation unit 4 through the third group of flow guiding pipes after being split through the annular groove 3101 of the heat exchange upper plate 31, and finally flows out from the cooling reaction product outlet 401 of the liquid-gas separation unit 4. The path taken by the initial hydrocarbon liquid fuel a and water B to the final gaseous reaction product D in the present reactor is as in fig. 1: a1, a a2→b→c d, e, f g, h, i, j, k.
The embodiments described above are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the embodiments described above, and any other changes, modifications, substitutions, combinations, and simplifications that do not depart from the spirit and principles of the present invention should be made in the equivalent manner, and are included in the scope of the present invention.
Claims (10)
1. An integrated hydrocarbon autothermal reforming hydrogen production reactor is characterized by comprising an evaporation unit, a catalytic reaction unit, a mixing and heat exchange unit and a liquid-gas separation unit which are connected in sequence, wherein:
The evaporation unit comprises an air inlet pipe, a heating rod and an evaporation body, wherein the heating rod is arranged in the evaporation body, the evaporation body is provided with a preheated liquid fuel inlet, an air and preheated fuel mixing channel and a mixed gaseous fuel outlet, two ends of the evaporation body are provided with fuel evaporation micro-channels, and the preheated liquid fuel inlet, the fuel evaporation micro-channels, the air and preheated fuel mixing channel and the mixed gaseous fuel outlet are sequentially communicated to form a fuel mixed evaporation flow channel;
the catalytic reaction unit comprises a reaction cylinder, a catalyst carrier and a heating ring, wherein a reaction cavity is arranged in the reaction cylinder, the heating ring is arranged on the outer side of the reaction cavity, the catalyst carrier is arranged at the bottom of the reaction cavity, a preheated liquid fuel conveying channel is arranged on one side of the reaction cylinder and is communicated with a preheated liquid fuel inlet, a mixed gaseous fuel inlet is arranged at the top of the reaction cylinder and is communicated with a mixed gaseous fuel outlet of the evaporation unit, and a reaction cylinder lower plate provided with a high-temperature reaction product outlet is arranged at the bottom of the reaction cylinder;
The mixing and heat exchanging unit comprises a heat exchanging sleeve, two ends of the heat exchanging sleeve are provided with a heat exchanging upper plate and a heat exchanging lower plate, a reaction product flow channel formed by a plurality of guide pipes is arranged in the heat exchanging sleeve, the heat exchanging upper plate is provided with a mixed liquid fuel outlet and an inlet of the reaction product flow channel, the inlet of the reaction product flow channel is communicated with a high-temperature reaction product outlet of the catalytic reaction unit, the mixed liquid fuel outlet is communicated with a preheated liquid fuel transportation channel of the catalytic reaction unit, the heat exchanging lower plate is provided with a reaction product flow channel outlet, two sides of the heat exchanging sleeve are provided with a hydrocarbon inlet and a water inlet, and a space between the heat exchanging sleeve and the guide pipes forms a mixing space of hydrocarbon and water;
The liquid-gas separation unit comprises a cooling reaction product outlet, a liquid collecting cavity and an outer cavity, wherein the liquid collecting cavity and the outer cavity are respectively communicated with a reaction product flow channel corresponding to the mixing and heat exchange unit, the liquid collecting cavity is provided with a liquid discharging hole for the separated liquid product to flow out, and the cooling reaction product outlet is communicated with the outer cavity.
2. The reactor for autothermal reforming of hydrocarbon according to claim 1, wherein thermocouples are disposed in both the evaporator and the reaction cartridge.
3. The reactor for autothermal reforming of hydrocarbon according to claim 1, wherein the upper end of the evaporator is provided with an evaporator upper plate, an evaporator upper gasket is provided between the evaporator upper plate and the evaporator for sealing, an evaporator lower gasket is provided between the evaporator and the catalytic reaction unit for sealing, and the mixed gaseous fuel outlet is provided at the center of the evaporator lower gasket.
4. The reactor for autothermal reforming of a hydrocarbon according to claim 1, wherein the fuel vaporization microchannel comprises an annular microchannel and a straight microchannel.
5. The reactor for autothermal reforming of a hydrocarbon according to claim 1, wherein the mixed gaseous fuel inlet and the high temperature reaction product outlet have tapered openings.
6. The reactor for autothermal reforming of hydrocarbon according to claim 1, wherein the reaction product flow channel is formed by flow ducts arranged outside the center of the heat exchange sleeve, the flow ducts are vertically arranged, one flow duct is arranged in the center of the heat exchange sleeve, the top of the flow duct is communicated with the inlet of the reaction product flow channel, the other flow ducts are symmetrically arranged on both sides of the flow duct in the center of the heat exchange sleeve, the flow ducts are communicated end to end, and the last flow duct is communicated with the outlet of the reaction product flow channel.
7. A reactor for autothermal reforming of a hydrocarbon in accordance with claim 6, wherein the heat exchange upper plate is provided with an annular recess and the heat exchange lower plate is provided with a circular recess.
8. A reactor for autothermal reforming of hydrocarbons in accordance with any one of claims 1-7, wherein the evaporation unit, catalytic reaction unit, mixing and heat exchange unit, and liquid-gas separation unit are each provided with a flange structure.
9. The reactor for autothermal reforming of hydrocarbon according to claim 7, wherein the flow guide tubes are divided into three groups, the flow guide tube at the center is arranged as a first group, the flow guide tube is arranged as a second group and a third group along one side of the center outwards, the lower end of the first group is communicated with the lower end of the second group through the circular groove of the heat exchange lower plate, and the upper end of the second group is communicated with the upper end of the third group through the annular groove of the heat exchange upper plate.
10. The reactor for autothermal reforming of hydrocarbon according to claim 9, wherein the plenum communicates with the lower ends of the first and second sets of draft tubes and the outer plenum communicates with the lower ends of the third set of draft tubes.
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