CN111661818A - Integrated hydrogen production reactor for autothermal reforming of hydrocarbon - Google Patents
Integrated hydrogen production reactor for autothermal reforming of hydrocarbon Download PDFInfo
- Publication number
- CN111661818A CN111661818A CN202010413922.0A CN202010413922A CN111661818A CN 111661818 A CN111661818 A CN 111661818A CN 202010413922 A CN202010413922 A CN 202010413922A CN 111661818 A CN111661818 A CN 111661818A
- Authority
- CN
- China
- Prior art keywords
- heat exchange
- unit
- evaporation
- liquid
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1276—Mixing of different feed components
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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 the normal vaporization of fuel; the catalytic reaction unit comprises a reaction cylinder, a catalyst carrier, a heating ring and a thermocouple, and the catalytic reaction of the fuel is ensured to be normally carried out; a reaction product flow channel and a liquid fuel mixing closed space are arranged in the mixing and heat exchange unit, and the mixing and heat exchange unit realizes the mixing and preheating of the fuel; and a liquid collecting cavity and a liquid discharging hole are arranged in the liquid-gas separation unit and are used for separating liquid and gaseous reaction products. The invention has the characteristics of integrating the functions of mixing, evaporation, catalytic reaction, heat exchange and liquid-gas separation into a whole 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 is the best choice for the mobile power supply because of the advantages of low working temperature, rapid start, high working current, large specific power energy density, no corrosion, zero noise, zero pollution, long service life and the like.
At present, a direct hydrogen storage mode is generally adopted for the fuel cell, but the problems of low energy density, large volume, dangerous storage and transportation and the like exist in the direct hydrogen storage mode, and the development of the fuel cell is seriously limited. On-site hydrogen production is considered to be one of the ways that the problem of direct hydrogen storage can be effectively solved, namely, liquid hydrocarbon with high energy density is adopted to generate hydrogen on site through a reaction system for supplying the hydrogen to a fuel cell. At present, hydrogen production methods present a diversified pattern, and the preparation of hydrogen by reforming hydrocarbons is a research hotspot in the field.
Typical hydrocarbon reforming reactions to produce hydrogen can be divided into three categories: steam reforming, partial oxidation reforming and autothermal reforming,
the steam reforming method can obtain hydrogen gas of higher purity, but the 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 carried out at lower temperatures, but the purity of the hydrogen is relatively low. The autothermal reforming method combines steam reforming and partial oxidation reforming together, and can obtain hydrogen with higher purity without external heat supply after reaction starting, so that the autothermal reforming reaction hydrogen production is a research hotspot.
Because the hydrocarbon autothermal reforming reaction comprises the processes of mixing, evaporation, catalytic reaction, heat exchange, liquid-gas separation and the like, each functional module of most reforming hydrogen production reactors is independent at present, so that the whole reaction system is large in size, and the heat loss in the reaction process is serious. Aiming at the problem, the invention provides the hydrocarbon autothermal reforming hydrogen production reactor which integrates the functions of mixing, evaporation, catalytic reaction, heat exchange and liquid-gas separation, and the invention has compact structure and improves the heat utilization rate of a reaction system.
Disclosure of Invention
In order to overcome the defects and shortcomings of 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 hydrogen production reactor for autothermal reforming of hydrocarbon 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 and an evaporation body, 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, the 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, 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 in the reaction cavity, a preheating liquid fuel transportation channel is arranged on one side of the reaction cylinder and is communicated with a preheating 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 exchange unit comprises a heat exchange sleeve, wherein a heat exchange upper plate and a heat exchange lower plate are arranged at two ends of the heat exchange sleeve, a reaction product flow channel consisting of a plurality of flow guide pipes is arranged in the heat exchange sleeve, a mixed liquid fuel outlet and an inlet of the reaction product flow channel are arranged on the heat exchange upper plate, 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 exchange lower plate is provided with a reaction product flow channel outlet, a hydrocarbon inlet and a water inlet are arranged at two sides of the heat exchange sleeve, and a space between the heat exchange sleeve and the flow guide pipes forms a mixing space of the hydrocarbon and the water;
the liquid-gas separation unit comprises a cooling reaction product outlet, a liquid collecting cavity and an outer cavity, 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 discharge 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 evaporation body upper end sets up the evaporation upper plate, it is used for sealing to set up evaporation body upper gasket between evaporation upper plate and the evaporation body, it is used for sealing to set up evaporation body lower gasket between evaporation body and the catalytic reaction unit, the mixed gaseous fuel export sets up the central point that puts at evaporation body lower gasket.
The fuel-evaporating microchannel includes an annular microchannel and a straight microchannel.
The mixed gaseous fuel inlet and the high temperature reaction product outlet have tapered openings.
The reaction product flow channel is composed of guide pipes which are arranged outwards from the center of the heat exchange sleeve, the guide pipes are vertically arranged, the guide pipe positioned at the center of the heat exchange sleeve is one, the top of the guide pipe is communicated with the inlet of the reaction product flow channel, other guide pipes are symmetrical by taking the guide pipe positioned at the center of the heat exchange sleeve and are uniformly arranged towards two sides, the guide pipes are communicated end to end, and the guide pipes in the last group 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 divide into three groups, and the honeycomb duct that sets up the center is first group, is second group and third group respectively along outside one side in center, the lower extreme of first group is through the circular recess of heat transfer hypoplastron and the lower extreme intercommunication of second group, the upper end of second group is through the annular groove of heat transfer upper plate and the upper end intercommunication of third group.
Preferably, the liquid collecting cavity is communicated with the lower ends of the first group of flow guide pipes and the second group of flow guide pipes, and the outer cavity is communicated with the lower ends of the third group of flow guide pipes.
The working process of the invention is as follows: the liquid hydrocarbon fuel A and water B in the mixing and heat exchange unit are mixed in the mixing and heat exchange unit and further preheated by heat exchange with the gaseous reaction product D, the preheated mixed liquid fuel A and B flow into the evaporation unit, the preheated mixed liquid fuel A and B are vaporized by heating of the heating rod and mixed with air C, and the resulting mixed gaseous fuel 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 the moment, the mixed gaseous fuel A, B and C in the catalytic reaction unit generate an autothermal reforming hydrogen production reaction under the combined action of the temperature and the catalyst to generate hydrogen and a small amount of byproducts, when the autothermal reforming reaction is carried out, the heat supply of the heating ring is stopped, and the obtained gaseous reaction product D flows into the mixing and heat exchange unit;
and the gaseous reaction product D in the mixing and heat exchange unit exchanges heat with the mixed liquid fuels A and B, the gaseous reaction product D after heat exchange flows into the liquid-gas separation unit, part of the reaction product is liquefied after meeting cold and flows into a liquid collection 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 cooled reaction product outlet.
The invention has the beneficial effects that:
(1) the invention can produce hydrogen with high purity and less impurities by autothermal reforming, can be used on site, has the concentration not reaching the explosion limit, has better safety and solves the problem of hydrogen storage.
(2) The invention recovers the waste heat of the reaction product to preheat the fuel, heats the liquid fuel and cools the reaction product at the same time, 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, evaporation, catalytic reaction, heat exchange and liquid-gas separation, can increase or reduce the number of each unit according to the requirement, and can adapt to scale expansion and scale reduction.
Drawings
FIG. 1 is a schematic diagram of the configuration of an integrated autothermal reforming hydrogen production reactor for hydrocarbons in accordance with the present invention;
FIG. 2 is a schematic diagram of a mixing and heat exchange unit according to an embodiment of the present invention;
FIG. 3 is a top view of the heat exchange upper plate of the mixing and heat exchange unit in an embodiment of the present invention;
FIG. 4 is a bottom view of a lower plate for exchanging heat with a mixing and heat exchange unit in an embodiment of the present invention;
FIG. 5 is a schematic structural view of an evaporation unit in an embodiment of the present invention;
FIG. 6 is a top view of an evaporation body of an evaporation unit in an embodiment of the present invention;
FIG. 7 is a bottom view of an evaporation body of an evaporation unit in an embodiment of the present invention;
FIG. 8 is a schematic structural view of a catalytic reaction unit in an embodiment of the present invention;
FIG. 9 is a top view of a reaction cartridge of a catalytic reaction unit in an embodiment of the present invention;
FIG. 10 is a top view of a liquid-gas separation unit in an embodiment of the present invention.
Detailed Description
The present invention will be described in further detail with reference to examples and drawings, but the present invention is not limited to these examples.
Examples
Referring to fig. 1, an integrated hydrocarbon autothermal reforming hydrogen production reactor integrates functions of mixing, evaporation, catalytic reaction, heat exchange and liquid-gas separation, and mainly comprises an evaporation unit 1, a catalytic reaction unit 2, a mixing and heat exchange unit 3 and a liquid-gas separation unit 4 which are sequentially connected.
Referring to fig. 1, 5, 6 and 7, the evaporation unit 1 includes an air inlet pipe 11, a short thermocouple connection pipe 12, a long thermocouple connection 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 both adopt flange structures, and through holes 106 for connecting bolts are arranged around the evaporation upper plate and the evaporation body for connecting the evaporation upper plate and the evaporation body with the catalytic reaction unit 2. An upper evaporator gasket 16 is disposed between the upper evaporator plate 14 and the evaporator 15 for sealing, and a lower evaporator gasket 17 is disposed between the evaporator 15 and the catalytic reaction unit 2 for sealing. The center of the lower gasket 17 of the evaporation body is provided with a mixed gaseous fuel outlet 102. And the two ends of the evaporation body are provided with fuel evaporation micro-channels comprising annular micro-channels and straight micro-channels. The evaporator 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. And a closed flow passage among the air inlet pipe 11, the evaporation body 15, the evaporation body upper gasket 16 and the evaporation body lower gasket 17 forms an evaporation channel of mixed fuel. The thermocouple junction pipe 12 is fixedly welded 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 connecting long pipe 13 is welded and fixed with the evaporation upper plate 14, and the long thermocouple is inserted and 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 a preheated liquid fuel inlet 101, flow into the annular micro-channel 104 through an 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 then flow into an air and preheated fuel mixing channel 103 through an outlet groove 108; meanwhile, the air C flows into the air-preheating fuel mixing passage 103 through the air intake duct 11, is mixed with the gaseous fuels a and B into the mixed gaseous fuels A, B and C, and then flows out from the mixed gaseous fuel outlet 102 of the evaporation body lower gasket 17 through the straight micro-passage 105, and the flow path of the mixed liquid fuels a and B in the evaporation unit 1 is 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 lower reaction cylinder plate 23 and a heating ring 24, the reaction cylinder 21 and the lower reaction cylinder plate 23 are both flange structures, through holes 205 for connecting bolts are uniformly distributed along the circumference for connecting with the evaporation unit 1 and the mixing and heat exchanging unit 3, and a gasket is placed between the reaction cylinder 21 and the lower reaction cylinder plate 23 for sealing and fixedly connected by bolts. The reaction cylinder 21 is provided with a preheated liquid fuel transportation channel 202; the inner space of the reaction cylinder 21 is a reaction chamber 201, a heating ring 24 is installed outside the reaction chamber 201, a catalyst carrier 22 is installed at the bottom in the reaction chamber 201, a mixed gaseous fuel inlet 203 is arranged at the top of the reaction chamber 201, and the mixed gaseous fuel inlet 203 is provided with a conical part with a downward opening, so that the mixed gaseous fuels A, B and C can be rapidly dispersed and uniformly flow through the catalyst carrier 22 when flowing in. The long thermocouple extends into the reaction chamber 201 through the mixed gaseous fuel inlet 203 and can monitor and control the temperature of the catalytic reaction unit 2. The lower plate 23 of the reaction cylinder is provided with a preheated liquid fuel transport passage 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, which is beneficial to rapidly collecting and flowing out the gaseous reaction product D obtained by the autothermal reforming hydrogen production reaction.
Referring to fig. 8 and 9, the operation process of the catalytic reaction unit 2 is as follows: the heating ring 24 heats the temperature inside the reaction chamber 201 to a preset reaction temperature in advance, then the mixed gaseous fuel A, B and C enters the reaction chamber 201 from the mixed gaseous fuel inlet 203, under the combined action of the temperature and the catalyst, the mixed gaseous fuel A, B and C undergoes an autothermal reforming reaction to generate hydrogen and a small amount of by-products, the heat supply 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 transport passage 202 of the catalytic reaction unit 2.
Referring to fig. 1, 2, 3 and 4, the mixing and heat exchanging unit 3 includes a heat exchanging upper plate 31, a heat exchanging sleeve 32, a heat exchanging lower plate 34 and a draft tube 33. Wherein, a mixed liquid fuel outlet 303 is arranged on the heat exchange upper plate 31; the heat exchange upper plate 31 and the heat exchange lower plate 34 are of flange structures, and through holes 306 which are uniformly distributed and used for connecting bolts are formed in the periphery of the heat exchange upper plate and the periphery of 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. A reaction product flow passage 304 formed by connecting a plurality of flow guide pipes 33 is arranged in the heat exchange sleeve 32 and is used for flowing the gaseous reaction product 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 the 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 an angle of 180 degrees.
Referring to fig. 2, 3 and 4, in the mixing and heat exchange unit 3, the reaction product flow passage 304 is composed of three sets of vertical guide pipes arranged outward from the center of the heat exchange sleeve 32, i.e., a first set, a second set and a third set, respectively, from the center to the outside, wherein the center set includes one guide pipe, the remaining sets include a plurality of guide pipes 33 arranged uniformly in the circumferential direction, and the diameter of the guide pipe near the center is larger than that of the guide pipe near the outside. The multiple groups of guide 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 sufficient heat exchange is realized. Specifically, the center of the heat exchange upper plate 31 is provided with a through hole for installing the guide pipe 33, and the end of the corresponding 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 mounting the draft tube 33, and the end parts of the corresponding draft tubes 33 are inserted into the through holes and welded and fixed. A circular groove 3401 is formed in the center of the lower surface of the heat exchange lower plate 34, a plurality of through holes for installing the guide pipes 33 are formed in the bottom of the circular groove 3401, and the end parts of the corresponding guide pipes 33 are inserted into the through holes and are welded and fixed; a plurality of through holes for installing the draft tube 33 are formed in the outer circle of the circular groove 3401 of the heat exchange lower plate 34, and the end of the corresponding draft tube 33 is inserted into the through holes and welded and fixed. The upper ends of the first group of draft tubes form the reaction product flow passage inlet 305, the lower ends thereof are communicated with the lower ends of the second group of draft tubes through the circular grooves 3401 on the heat exchange lower plate 34, the upper ends of the second group of draft tubes are communicated with the upper ends of the third group of draft tubes through the annular grooves 3101 on the heat exchange upper plate 31, and the lower ends of the third group of draft tubes form the reaction product flow passage outlet 308, thereby forming the reaction product flow passage 304.
Referring to fig. 2, 3 and 4, the operation of the mixing and heat exchanging unit 3 is as follows: on one hand, the gaseous reaction product D obtained by the autothermal reforming reaction of the catalytic reaction unit 2 and mixed with hydrogen and the like 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 end plate through the second group of flow guide pipes, flows out after finally flowing to the heat exchange lower plate 34 through the third group of flow guide pipes, and the flow path of the gaseous reaction product D in the mixing and heat exchange unit 3 is g → h → i → j; meanwhile, 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 to be mixed, the guide pipe 33 is soaked in the mixed liquid fuels a and B, so that the heat of the high-temperature reformed gas flowing through the guide pipe 33 is transferred to the mixed liquid fuels a and B with lower temperature for preheating, preparation is made for the subsequent vaporization of the mixed liquid fuels a and B in the evaporation unit 1, and 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 fuel a and the water B in the mixing and heat exchange unit 3 are a1, a2 → B → c.
Referring to fig. 10, the liquid-gas separation unit 4 is provided in a flange structure, and is provided with through holes 405 for bolts connected to the mixing and heat exchange unit 3 at the periphery. The liquid-gas separation unit 4 is provided with a liquid collecting cavity 402 and an outer cavity 403, the liquid collecting cavity 402 is provided with a liquid discharging hole 404 for discharging separated liquid products; the side surface of the liquid-gas separation unit 4 is provided with a cooled reaction product outlet 401 which is communicated with an outer cavity 403.
Referring to fig. 1 to 10, in the hydrocarbon autothermal reforming hydrogen production reactor which integrates the functions of mixing, evaporation, catalytic reaction, heat exchange and liquid-gas separation and constitutes the present embodiment, the air inlet pipe 11 is communicated with the air and preheated fuel mixing channel 103 of the evaporation unit 1; the mixing enclosed space 302 of the mixing and heat exchanging unit 3 is communicated with the preheating liquid fuel transportation channel 202 of the catalytic reaction unit 2, the preheating 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 exchanging unit 3, and the liquid collecting chamber 402 and the outer chamber 403 of the liquid-gas separation unit 4 in sequence, specifically, the overlapping relationship and alignment of the respective units are as follows:
the evaporation unit 1 is arranged on the catalytic reaction unit 2, and a preheated liquid fuel inlet 101 of the evaporation unit 1 is aligned and communicated with a preheated liquid fuel conveying channel 202 of the catalytic reaction unit 2; the mixed gaseous fuel outlet 102 of the vaporizing unit 1 is in aligned communication with the mixed gaseous fuel inlet 203 of the catalytic reaction unit 2; the plurality of connecting screw through holes 106 of the evaporation unit 1 are aligned and communicated with the connecting screw through holes 205 of the catalytic reaction unit 2, respectively, 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 preheating 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 aligning way; 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 plurality of connecting screw through holes 205 of the catalytic reaction unit 2 are aligned and communicated with the plurality of connecting screw through holes 306 of the mixing and heat exchanging unit 3, respectively, and the two units are locked by bolts with a graphite gasket (not shown) interposed therebetween.
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 cooled reaction product outlet 401 of the liquid-gas separation unit 4 on the same side, the plurality of through holes 306 for connecting threads of the mixing and heat exchange unit 3 are respectively aligned and communicated with the plurality of through holes 405 for connecting threads of the liquid-gas separation unit 4, the mixing and heat exchange unit is used for connecting the two units through bolt locking, and a graphite gasket is placed between the two units for sealing (not shown in the figure).
Referring to fig. 1 to 10, the hydrocarbon autothermal reforming hydrogen production reactor integrating the functions of mixing, evaporation, catalytic reaction, heat exchange and liquid-gas separation operates as follows:
in practice, the hydrocarbon liquid fuel a and the water B enter from the liquid hydrocarbon inlet 301 and the water inlet 307 of the mixing and heat exchanging unit 3, respectively, and are mixed in the mixing enclosed space 302; the guide pipe of the mixing and heat exchanging unit 3 is soaked in the mixed liquid fuels A and B, so that the heat of a gaseous reaction product D flowing through the guide pipe of the mixing and heat exchanging unit 3 subsequently is transferred to the mixed liquid fuels A and B with lower temperature; then 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 exchanging 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 the air C in the air and preheated fuel mixing channel 103, and after the mixed gaseous fuels A, B and C flow out through the mixed gaseous fuel outlet 102, enter the reaction cavity 201 through the mixed gaseous fuel inlet 203 of the catalytic reaction unit 2, under the combined action of the heating ring 24 and the catalyst carrier 22, the autothermal reforming reaction is carried out to generate hydrogen and a small amount of byproducts, and when the autothermal reforming reaction is carried out, the heat supply of the heating ring 24 is stopped; the high-temperature gaseous reaction product D flows into the reaction product flow passage 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 flows into the liquid-gas separation unit 4 through the first group of draft tubes, liquid-gas separation is carried out in the liquid collection cavity 402, the gas after being divided flows into the heat exchange upper plate 31 through the second group of draft tubes, flows into the outer cavity 403 of the liquid-gas separation unit 4 through the third group of draft tubes after being divided by 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 followed in the present reactor by the initial hydrocarbon liquid fuel a and water B to the final gaseous reaction product D is as in fig. 1: a1, a2 → b → c → d → e → f → g → h → i → j → k.
The above embodiments are preferred embodiments of the present invention, but the present invention is not limited to the above embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be construed as equivalents thereof, and all such changes, modifications, substitutions, combinations, and simplifications are intended to be included in the scope of the present invention.
Claims (10)
1. The utility model provides an integrated hydrocarbon autothermal reforming hydrogen production reactor which characterized in that, includes evaporation unit, catalytic reaction unit, mixing and heat exchange unit and the liquid-gas separation unit that connect gradually, wherein:
the evaporation unit comprises an air inlet pipe, a heating rod and an evaporation body, 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, the 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, 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 in the reaction cavity, a preheating liquid fuel transportation channel is arranged on one side of the reaction cylinder and is communicated with a preheating 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 exchange unit comprises a heat exchange sleeve, wherein a heat exchange upper plate and a heat exchange lower plate are arranged at two ends of the heat exchange sleeve, a reaction product flow channel consisting of a plurality of flow guide pipes is arranged in the heat exchange sleeve, a mixed liquid fuel outlet and an inlet of the reaction product flow channel are arranged on the heat exchange upper plate, 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 exchange lower plate is provided with a reaction product flow channel outlet, a hydrocarbon inlet and a water inlet are arranged at two sides of the heat exchange sleeve, and a space between the heat exchange sleeve and the flow guide pipes forms a mixing space of the hydrocarbon and the water;
the liquid-gas separation unit comprises a cooling reaction product outlet, a liquid collecting cavity and an outer cavity, 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 discharge hole for separated liquid products to flow out, and the cooling reaction product outlet is communicated with the outer cavity.
2. The reactor of claim 1, wherein thermocouples are disposed in the evaporator and the reactor barrel.
3. The hydrocarbon autothermal reforming hydrogen production reactor of claim 1, wherein an upper evaporation plate is disposed at an upper end of the evaporation body, an upper evaporation body gasket is disposed between the upper evaporation plate and the evaporation body for sealing, a lower evaporation body gasket is disposed between the evaporation body and the catalytic reaction unit for sealing, and the mixed gaseous fuel outlet is disposed at a central position of the lower evaporation body gasket.
4. The hydrocarbon autothermal reforming hydrogen production reactor of claim 1, wherein the fuel-evaporating microchannels comprise annular microchannels and straight microchannels.
5. The hydrocarbon autothermal reforming hydrogen production reactor of claim 1, wherein the mixed gaseous fuel inlet and the high temperature reaction product outlet have tapered openings.
6. The hydrocarbon autothermal reforming hydrogen production reactor of claim 1, wherein the reaction product flow channel is formed by flow guide pipes arranged outward from the center of the heat exchange sleeve, the flow guide pipes are vertically arranged, one flow guide pipe is arranged at the center of the heat exchange sleeve, the top of the flow guide pipe is communicated with the inlet of the reaction product flow channel, the other flow guide pipes are symmetrically arranged at the center of the heat exchange sleeve and are uniformly arranged towards two sides, the flow guide pipes are communicated end to end, and the last group of flow guide pipes are communicated with the outlet of the reaction product flow channel.
7. The hydrocarbon autothermal reforming reactor of claim 6, wherein the heat exchange upper plate has an annular groove and the heat exchange lower plate has a circular groove.
8. The hydrocarbon autothermal reforming hydrogen production reactor of any one of claims 1-7, wherein the evaporation unit, the catalytic reaction unit, the mixing and heat exchange unit, and the liquid-gas separation unit are each provided with a flange structure.
9. The hydrocarbon autothermal reforming hydrogen production reactor of claim 7, wherein the flow conduits are divided into three groups, the flow conduits disposed in the center are a first group, and a second group and a third group are respectively disposed outwardly along one side of the center, 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 hydrocarbon autothermal reforming hydrogen production reactor of claim 9, wherein the liquid collection chamber is in communication with the lower ends of the first and second sets of flow conduits, and the outer chamber is in communication with the lower ends of the third set of flow conduits.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010413922.0A CN111661818A (en) | 2020-05-15 | 2020-05-15 | Integrated hydrogen production reactor for autothermal reforming of hydrocarbon |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010413922.0A CN111661818A (en) | 2020-05-15 | 2020-05-15 | Integrated hydrogen production reactor for autothermal reforming of hydrocarbon |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111661818A true CN111661818A (en) | 2020-09-15 |
Family
ID=72383834
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010413922.0A Pending CN111661818A (en) | 2020-05-15 | 2020-05-15 | Integrated hydrogen production reactor for autothermal reforming of hydrocarbon |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111661818A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113351144A (en) * | 2021-06-01 | 2021-09-07 | 上海交通大学 | Fuel catalytic reformer based on waste heat utilization |
| CN114249298A (en) * | 2022-02-24 | 2022-03-29 | 清华大学 | Methanol reformer and fuel cell |
| CN114784946A (en) * | 2022-04-27 | 2022-07-22 | 华南理工大学 | Data center composite power supply system combining field hydrogen production technology and control method |
-
2020
- 2020-05-15 CN CN202010413922.0A patent/CN111661818A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113351144A (en) * | 2021-06-01 | 2021-09-07 | 上海交通大学 | Fuel catalytic reformer based on waste heat utilization |
| CN113351144B (en) * | 2021-06-01 | 2022-10-18 | 上海交通大学 | Fuel catalytic reformer based on waste heat utilization |
| CN114249298A (en) * | 2022-02-24 | 2022-03-29 | 清华大学 | Methanol reformer and fuel cell |
| CN114249298B (en) * | 2022-02-24 | 2022-06-21 | 清华大学 | Methanol reformer and fuel cell |
| CN114784946A (en) * | 2022-04-27 | 2022-07-22 | 华南理工大学 | Data center composite power supply system combining field hydrogen production technology and control method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111661818A (en) | Integrated hydrogen production reactor for autothermal reforming of hydrocarbon | |
| US10773229B2 (en) | Steam reformers, modules, and methods of use | |
| CN109855107B (en) | Heat supply dehydrogenation integrated reactor | |
| CN112892460B (en) | Self-heating methanol reforming hydrogen production reactor | |
| CN112960647B (en) | Reforming hydrogen production and catalytic combustion integrated device with variable catalyst particle arrangement | |
| US11597649B2 (en) | Steam methane reformer hydrogen generation systems | |
| US20230339748A1 (en) | Solar-driven methanol reforming system for hydrogen production | |
| CN113930799A (en) | Heat recovery system for hydrogen production of solid oxide electrolytic cell | |
| CN110864287B (en) | Flat-plate micro heat pipe wall surface catalytic combustor | |
| CA3176087C (en) | Hydrogen generation systems | |
| CN212476104U (en) | Self-heating reforming hydrogen production reaction system integrating multiple functions | |
| CN106602111A (en) | Combustion reformer adopting high-temperature tail gas combustion for heat supply | |
| CN111453697B (en) | Multi-fuel universal reforming hydrogen production system and method for SOFC | |
| CN113813884A (en) | Safe and efficient reforming hydrogen production reactor | |
| CN115159454A (en) | Methanol reforming reactor with internal integrated evaporator | |
| CN211719720U (en) | Universal reforming fuel cell system | |
| CN212503986U (en) | Multi-return-stroke reforming hydrogen production reactor | |
| CN218931718U (en) | Self-heat-supply type tubular reactor for methanol reforming hydrogen production reaction | |
| CN217887946U (en) | Chloroethylene conversion system | |
| CN111346590B (en) | Integrated reactor | |
| RU2801525C1 (en) | Device for obtaining a hydrogen-containing mixture from ammonia | |
| CN114838352B (en) | Supercritical mixed working medium oxidation reactor coupled with spiral tube heat exchange | |
| US11891302B2 (en) | Hydrogen generation systems | |
| CN115121197A (en) | Chloroethylene conversion system | |
| CN116617995A (en) | Thermal coupling reaction unit and reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |