CN116477571B - Integrated hydrogen production reactor - Google Patents
Integrated hydrogen production reactor Download PDFInfo
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- CN116477571B CN116477571B CN202310356704.1A CN202310356704A CN116477571B CN 116477571 B CN116477571 B CN 116477571B CN 202310356704 A CN202310356704 A CN 202310356704A CN 116477571 B CN116477571 B CN 116477571B
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- hydrogen production
- fuel
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000001257 hydrogen Substances 0.000 title claims abstract description 39
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 103
- 239000000446 fuel Substances 0.000 claims abstract description 70
- 239000007921 spray Substances 0.000 claims abstract description 34
- 238000002485 combustion reaction Methods 0.000 claims abstract description 32
- 238000012545 processing Methods 0.000 claims abstract description 29
- 238000009834 vaporization Methods 0.000 claims abstract description 29
- 230000008016 vaporization Effects 0.000 claims abstract description 29
- 239000002918 waste heat Substances 0.000 claims abstract description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000003546 flue gas Substances 0.000 claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 10
- 239000002994 raw material Substances 0.000 claims description 21
- 238000002156 mixing Methods 0.000 claims description 14
- 238000010438 heat treatment Methods 0.000 claims description 13
- 239000002245 particle Substances 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 7
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 3
- 239000010931 gold Substances 0.000 claims description 3
- 229910052737 gold Inorganic materials 0.000 claims description 3
- 229910052709 silver Inorganic materials 0.000 claims description 3
- 239000004332 silver Substances 0.000 claims description 3
- 238000007084 catalytic combustion reaction Methods 0.000 abstract description 13
- 238000012546 transfer Methods 0.000 abstract description 10
- 239000003921 oil Substances 0.000 description 12
- 238000000034 method Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 238000005192 partition Methods 0.000 description 5
- 238000004321 preservation Methods 0.000 description 5
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- 229920000742 Cotton Polymers 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000001651 catalytic steam reforming of methanol Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000005485 electric heating Methods 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000002480 mineral oil Substances 0.000 description 2
- 235000010446 mineral oil Nutrition 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000010742 number 1 fuel oil Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
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
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
-
- 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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
-
- 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
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
- C01B2203/1223—Methanol
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides an integrated hydrogen production reactor, relates to the technical field of hydrogen production reactors, and aims to solve the problems that a device occupies a large area and combustible components in the device are not effectively utilized. The integrated hydrogen production reactor comprises: a reaction box; a fuel processing assembly installed inside the reaction tank; the separation plate is arranged in the reaction box and is used for separating the reaction box into a combustion chamber and a reaction chamber; the spray pipe is arranged in the combustion chamber; a catalyst filled in the combustion chamber; the vaporization superheater is arranged in the combustion chamber; the outlet of the reaction assembly is communicated with the inlet of the reaction assembly; a heat-conducting medium filled into the reaction chamber; and the two ends of the waste heat circulation assembly are respectively communicated with the air outlet end of the combustion chamber and the fuel treatment assembly. The invention adopts catalytic combustion to provide the heat required by the equipment, and reduces the equipment for supplying heat conduction oil; the heat transfer efficiency is improved by filling the heat transfer medium in the gap inside the device; the reacted flue gas is recycled, so that the heat loss is reduced, and the cost is saved.
Description
Technical Field
The invention relates to the technical field of hydrogen production reactors, in particular to an integrated hydrogen production reactor.
Background
The whole device needs an external heat source, the existing methanol steam reforming hydrogen production device widely adopts a heat conduction oil system as a heat source, the heat conduction oil is used as a heat carrier, generally the heat conduction oil is heated to 290 ℃ and then enters the methanol steam reforming system, after providing heat for the system, the temperature of the heat conduction oil is reduced to about 270 ℃ and returns to a heat conduction oil furnace, and a closed heat conduction oil circulation heating system is formed. The heat conduction oil system mostly adopts an open fire heating device (such as fire coal or fuel oil, gas and the like), and the heat conduction oil generally adopts mineral oil (model is WD-320), so that the mineral oil is easy to be carbonized, and all pipelines and equipment of the whole heat conduction oil system must be cleaned for 2-3 years, thereby increasing the cost; in addition, according to relevant national regulations, the safety distance between the open fire device and the hydrogen device is not smaller than 15m, and the heat conduction oil system occupies a larger area, so that the occupied area of the whole methanol steam reforming hydrogen production device is large, and the requirements of the volume and the occupied area of the microminiature methanol hydrogen production device are not met to a great extent; in addition, the combustible components in the tail gas are not effectively utilized, so that resource waste is caused.
Disclosure of Invention
The invention provides an integrated hydrogen production reactor for solving the technical problems, which adopts catalytic combustion to provide heat for equipment and reduces equipment for supplying heat conduction oil; the heat transfer efficiency is improved by filling the heat transfer medium in the gap inside the device; the reacted flue gas is recycled, so that the heat loss is reduced, and the cost is saved.
The technical scheme adopted by the invention is as follows:
an integrated hydrogen production reactor comprising:
A reaction box;
the fuel treatment assembly is arranged in the reaction box, and the air inlet end of the fuel treatment assembly extends out of the reaction box;
the separation plate is arranged in the reaction box and sleeved outside the fuel processing assembly, a combustion chamber is formed between the separation plate and the fuel processing assembly, and a reaction cavity is formed between the separation plate and the inner side wall of the reaction box;
The spray pipe is vertically arranged in the combustion chamber, one end of the spray pipe is communicated with the fuel processing assembly, and a plurality of spray holes of the spray pipe are arranged along the axial direction of the spray pipe;
a catalyst filled in the combustion chamber;
The vaporization superheater is arranged in the combustion chamber, and a feed inlet of the vaporization superheater is positioned outside the reaction box;
The reaction component is arranged in the reaction cavity, and the outlet of the vaporization superheater is communicated with the inlet of the reaction component;
A heat-conducting medium filled into the reaction chamber;
and one end of the waste heat circulation assembly is communicated with the flue gas outlet of the integrated hydrogen production reactor, and the other end of the waste heat circulation assembly is connected to the gas inlet of the fuel treatment assembly.
Optionally, the fuel processing assembly comprises:
An inner sleeve arranged in the reaction box;
The outer sleeve is sleeved outside the inner sleeve, a mixing area is formed between the outer sleeve and the inner sleeve, the air outlet end of the waste heat circulation assembly is connected into the outer sleeve, and the inlet of the spray pipe is connected into the mixing area;
and one end of the fuel feeding pipe extends into the inner sleeve and is communicated with the mixing area, and the other end of the fuel feeding pipe is positioned outside the reaction box.
Optionally, the plurality of nozzles are uniformly disposed about the fuel processing assembly.
Optionally, when the plurality of spray holes arranged along the axis direction of the spray pipe are a group, the spray pipe is provided with a plurality of groups of spray holes along the circumferential direction of the spray pipe.
Optionally, the vaporization superheater comprises
The first annular pipe is sleeved outside the fuel treatment assembly, and a raw material inlet is arranged on the first annular pipe;
the second annular pipe is sleeved outside the fuel treatment assembly, and a raw material outlet is arranged on the second annular pipe;
The inner coil pipe is sleeved outside the fuel treatment assembly, and two ends of the inner coil pipe are respectively communicated with the first annular pipe and the second annular pipe;
The outer coil pipe is sleeved outside the inner coil pipe, and two ends of the outer coil pipe are respectively communicated with the first annular pipe and the second annular pipe;
wherein the nozzle, when installed, is positioned between the inner coil and the outer coil.
Optionally, the reaction assembly comprises:
The reaction tubes are arranged in the reaction cavity at equal intervals;
And one end of the air inlet pipe is communicated with the outlet of the vaporization superheater, and the other end of the air inlet pipe is connected into the reaction pipe.
Optionally, the heat conducting medium is aluminum particles, copper particles, silver particles or gold particles.
Optionally, at least one auxiliary heating device is arranged in the combustion chamber.
Optionally, the reaction box, the fuel processing assembly, the partition plate, the spray pipe, the vaporization superheater, the reaction assembly and the waste heat circulation assembly are of an integrated structure.
Optionally, an insulating layer is arranged on the outer side of the reaction box.
Compared with the prior art, the invention has the beneficial effects that:
1. The invention does not adopt the existing heat conduction oil heating mode any more, and directly adopts catalytic combustion to provide the heat required by the whole equipment, thereby reducing the volume of the equipment.
2. The heat-conducting medium is filled in the gap inside the equipment, so that the heat transfer efficiency is improved; the smoke is recycled, so that heat loss is reduced, and cost is saved.
3. The vaporization superheater adopts a double-layer spiral coil structure, so that the vaporization stroke is long enough, and the vaporization superheating requirement is met; the vaporization superheater is integrated in the combustion chamber of the equipment body, so that the heat transfer time, the heat transfer process and the heat transfer loss are reduced, and the vaporization superheating effect is optimized; meanwhile, the whole volume of the equipment is reduced, and the occupied area is reduced.
4. The invention adopts the mode of preheating and then injecting the fuel, so that the fuel can be uniformly injected along the spray hole of the spray pipe, the overall temperature can be uniformly increased, and the situations of local temperature flying and the like are reduced.
5. The auxiliary heating device is arranged in the combustion chamber, so that the auxiliary heating device can be preheated at low temperature, and can stably maintain the constant temperature in standby, thereby reducing the temperature rise time when equipment is operated each time; the hot start machine can be started at any time, so that the machine starting time is greatly shortened, and a large amount of time cost is saved.
6. The outermost side of the invention is wrapped by heat insulation cotton to insulate heat, thereby reducing heat loss.
7. The invention greatly reduces the whole volume of the hydrogen production system, lightens the whole weight of the system and integrates the whole system into a whole.
Drawings
In order to more clearly illustrate the embodiments of the application or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of the internal structure of an integrated hydrogen production reactor.
Fig. 2 is a schematic perspective view of a partial structure of an integrated hydrogen production reactor.
FIG. 3 is a schematic cross-sectional view of the internal structure of an integrated hydrogen production reactor.
FIG. 4 is a schematic structural view of a nozzle of an integrated hydrogen production reactor.
FIG. 5 is a schematic diagram of an integrated hydrogen production reactor with a heat preservation layer.
FIG. 6 is a schematic diagram of an integrated hydrogen production reactor with an auxiliary heating device.
Reference numerals:
1. a reaction box; 11. a combustion chamber; 12. a reaction chamber;
2. a fuel processing assembly; 21. an inner sleeve; 22. a fuel feed pipe; 23. an outer sleeve; 24. a mixing region;
3. A partition plate; 31. a porous metal annular bottom plate;
4. A spray pipe; 41. a spray hole;
5. A catalyst;
6. A vaporization superheater; 61. a first collar; 62. a raw material inlet; 63. a second loop; 64. a raw material outlet; 65. an inner coil; 66. an outer coil;
7. A reaction assembly; 71. a reaction tube; 72. an air inlet pipe;
8. A heat-conducting medium;
9. A waste heat recycling assembly;
10. An auxiliary heating device;
110. A heat preservation layer;
120. And an outer pipeline.
Detailed Description
Hereinafter, only certain exemplary embodiments are briefly described. As will be recognized by those of skill in the pertinent art, the described embodiments may be modified in various different ways without departing from the spirit or scope of the present invention. Accordingly, the drawings and description are to be regarded as illustrative in nature and not as restrictive.
In the description of the present invention, it should be understood that the terms "upper", "lower", "top", "bottom", "inner", "outer", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on those shown in the drawings, or orientations or positional relationships conventionally put in use of the product of the present invention, or orientations or positional relationships conventionally understood by those skilled in the art, are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; the device can be mechanically connected, electrically connected and communicated; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is less level than the second feature.
The following disclosure provides many different embodiments, or examples, for implementing different features of the invention. In order to simplify the present disclosure, components and arrangements of specific examples are described below. They are, of course, merely examples and are not intended to limit the invention. Furthermore, the present invention may repeat reference numerals and/or letters in the various examples, which are for the purpose of brevity and clarity, and which do not themselves indicate the relationship between the various embodiments and/or arrangements discussed. In addition, the present invention provides examples of various specific processes and materials, but one of ordinary skill in the art will recognize the application of other processes and/or the use of other materials.
Embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
As shown in fig. 1,2 and 3, an embodiment of the present invention provides an integrated hydrogen production reactor, comprising: the device comprises a reaction box 1, a fuel processing assembly 2, a partition plate 3, a spray pipe 4, a catalyst 5, a vaporization superheater 6, a reaction assembly 7, a heat conducting medium 8 and a waste heat circulation assembly 9.
The fuel processing assembly 2 is installed inside the reaction tank 1, and its air inlet end extends to the outside of the reaction tank 1. The separation plate 3 is arranged in the reaction box 1 and sleeved outside the fuel processing assembly 2, a combustion chamber 11 is formed between the separation plate 3 and the fuel processing assembly 2, and a reaction cavity 12 is formed between the separation plate 3 and the inner side wall of the reaction box 1. The nozzle 4 is vertically installed in the combustion chamber 11, one end of the nozzle 4 is communicated with the fuel processing assembly 2, and a plurality of spray holes 41 of the nozzle 4 are arranged along the axial direction of the nozzle 4. The catalyst 5 is filled in the combustion chamber 11. The vaporization superheater 6 is installed in the combustion chamber 11, and its feed port is located outside the reaction tank 1. A reaction assembly 7 is mounted in the reaction chamber 12, and the outlet of the vaporization superheater 6 is in communication with the inlet of the reaction assembly 7. The heat-conducting medium 8 is filled into the reaction chamber 12. One end of the waste heat circulation assembly 9 is communicated with a flue gas outlet of the integrated hydrogen production reactor, and the other end of the waste heat circulation assembly is connected to an air inlet of the fuel processing assembly 2.
The fuel is conveyed into the fuel processing assembly 2, the flue gas and the fuel which are sent into the reaction tank 1 through the waste heat circulation assembly 9 are uniformly mixed in the fuel processing assembly 2, then enter the spray pipe 4, and are sprayed out through the spray hole 41 of the spray pipe 4 to perform catalytic combustion with the catalyst 5 filled in the combustion chamber 11. Raw materials enter the vaporization superheater 6 through a feed pipe, and as the vaporization superheater 6 is arranged in the combustion chamber 11, heat generated during catalytic combustion is absorbed when the raw materials pass through the combustion chamber 11, the raw materials are preheated in the vaporization superheater 6, enter the reaction component 7 for full reaction after being preheated, and gas after reaction is discharged and collected intensively. The fuel and the catalyst 5 are discharged outside the flue gas generated in the catalytic combustion process, and the flue gas of the integrated hydrogen production reactor is circulated into the fuel treatment assembly 2 through the waste heat circulation assembly 9 for secondary use.
The heat generated in the catalytic combustion process is partially absorbed by the raw materials in the vaporization superheater 6, the other part is transferred to the heat conducting medium 8 in the reaction cavity 12 through the partition plate 3, and the heat conducting medium 8 transfers the heat to the reaction component 7, so that the preheated raw materials are rapidly and fully reacted in the reaction component 7. The flue gas generated in the catalytic combustion process has certain heat, so that the waste of the heat is avoided, and the heat is circulated into the reaction cavity for heat exchange. The flue gas generated in the reaction process of the integrated hydrogen production reactor is circulated into the fuel processing assembly 2 through the waste heat circulation assembly 9, so that the temperature of fuel is increased, and the reaction speed of catalytic combustion is increased.
The flue gas generated in the reaction process contains combustible gas and has a certain temperature, so that the flue gas is recycled. And after the flue gas is catalyzed and combusted, the rest heat is absorbed and discharged.
The bottom of the combustion chamber 11 is provided with a catalyst 5 outlet, and a flange is arranged at the catalyst 5 outlet and is sealed, so that the combustion chamber 11 forms a closed chamber. The flange is provided inside with a porous metal annular bottom plate 31 for supporting the catalyst 5.
In another embodiment, as shown in fig. 1,2 and 3, the fuel processing assembly 2 includes: an inner sleeve 21, a fuel feed tube 22, and an outer sleeve 23; the inner jacket tube 21 is mounted in the reaction tank 1. The outer sleeve 23 is sleeved outside the inner sleeve 21, a mixing area 24 is formed between the outer sleeve 23 and the inner sleeve 21, the air outlet end of the waste heat circulation assembly 9 is connected into the outer sleeve 23, and the inlet of the spray pipe 4 is connected into the mixing area 24. One end of the fuel feed pipe 22 extends into the inner sleeve 21 and is communicated with the mixing area 24, the other end of the fuel feed pipe is positioned outside the reaction tank 1, and one end extending out of the reaction tank 1 is connected with a fuel storage device, so that fuel can be conveniently provided for the inner sleeve 21. The inlet height of the fuel feed pipe 22 into the mixing zone 24 is higher than the inlet height of the waste heat recycling assembly 9 in order to allow the fuel to be thoroughly mixed with the flue gas with waste heat in the mixing zone.
The flue gas generated during the reaction of the integrated hydrogen production reactor circulates into the outer sleeve 23 through the waste heat circulation assembly 9, and is mixed with fuel in the mixing area 24 between the outer sleeve 23 and the inner sleeve 21, so that the fuel has partial heat, the mixed fuel enters the spray pipe 4, and is uniformly sprayed into the combustion chamber 11 through the spray holes 41 arranged on the spray pipe 4. The waste heat of the flue gas is recycled, so that the temperature of the fuel in the fuel treatment assembly 2 can be increased, and the heat loss is reduced.
It should be noted that, the thickness of the inner sleeve 21 is greater than that of the outer sleeve 23, and the inner sleeve 21 plays a certain supporting role in the reaction tank 1, and simultaneously facilitates the installation of the fuel feed pipe 22 and the waste heat circulation assembly 9.
In another embodiment, as shown in FIG. 2, the plurality of nozzles 4 are uniformly disposed about the fuel processing assembly 2 in order to provide more uniform fuel injection within the combustion chamber 11.
In another embodiment, as shown in fig. 4, the fuel is uniformly injected along the injection pipe, so that the overall temperature of the integrated hydrogen production reactor can be uniformly increased, and the situations such as local temperature runaway and the like are reduced; when a plurality of injection holes 41 are provided in a group along the axial direction of the nozzle 4, the nozzle 4 is provided with a plurality of groups of injection holes 41 along the circumferential direction thereof.
In another embodiment, as shown in fig. 2 and 3, the vaporization superheater 6 includes: the first annular pipe 61, the second annular pipe 63, the inner coil pipe 65 and the outer coil pipe 66, the first annular pipe 61 is sleeved outside the fuel processing assembly 2, and the first annular pipe 61 is provided with a raw material inlet 62. The second annular pipe 63 is sleeved outside the fuel processing assembly 2, and a raw material outlet 64 is arranged on the second annular pipe 63. An inner coil 65 is sleeved outside the fuel processing assembly 2, and two ends of the inner coil are respectively communicated with the first annular pipe 61 and the second annular pipe 63. The outer coil 66 is sleeved outside the inner coil 65, and two ends of the outer coil are respectively communicated with the first annular pipe 61 and the second annular pipe 63. Wherein said nozzle 4, when installed, is positioned between said inner coil 65 and said outer coil 66.
When the raw materials enter the first annular pipe 61 and are distributed into the inner coil pipe 65 and the outer coil pipe 66, the raw materials are preheated in the inner coil pipe 65 and the outer coil pipe 66, and as the inner coil pipe 65 and the outer coil pipe 66 are arranged in the combustion chamber 11, part of heat can preheat the raw materials in the coil pipes during the catalytic combustion reaction, the preheated raw materials are converged into the second annular pipe 63, and the raw materials enter the reaction assembly 7 through the raw material outlet 64 on the second annular pipe 63 for reaction. The time required for the reaction can be reduced as the feedstock is preheated in the inner coil 65 and the outer coil 66.
In another embodiment, as shown in fig. 1, 2 and 3, the reaction module 7 includes: the reaction tube 71 and the air inlet tube 72 are provided in plural, equally spaced, reaction chamber 12. The number of the air inlet pipes 72 is matched with that of the reaction pipes 71, one end of each air inlet pipe 72 is communicated with the outlet of the vaporization superheater 6, and the other end of each air inlet pipe 72 is connected into the reaction pipe 71.
One end of the air inlet pipe 72 is connected to the raw material outlet 64 of the second loop pipe 63, and the other end is connected to the reaction pipe 71. The preheated raw materials are fed into the reaction tube 71 for reaction. The gas obtained by the reaction is discharged through the outlet at the other end of the reaction tube 71.
In one embodiment, the tubes of the reaction tube 71 are spirally arranged to increase the residence time of the feedstock in the reaction tube 71 for more complete reaction.
In another embodiment, the outer side wall of the reaction tube 71 may be provided with a convex or concave structure, so as to increase the contact area between the heat conducting medium 8 and the reaction tube 71.
In another embodiment, the heat conducting medium 8 is aluminum particles, copper particles, silver particles or gold particles in order to facilitate the transfer of the heat of the catalytic combustion reaction to the reaction tube 71. Wherein the optimal aluminum particles are used at a lower cost.
In another embodiment, as shown in fig. 6, at least one auxiliary heating device 10 is disposed in the combustion chamber 11. The auxiliary heating device 10 is an electric heating rod, adopts the electric heating rod to assist in heating, can preheat at low temperature, can stably maintain the constant temperature in standby, reduces the heating time in each equipment operation, and ensures that the cooling machine is heated to the required temperature for a short time. The hot start machine can be started at any time, so that the machine starting time is greatly shortened, and a large amount of time cost is saved.
In another embodiment, the reaction tank 1, the fuel processing assembly 2, the partition plate 3, the spray pipe 4, the vaporization superheater 6, the reaction assembly 7 and the waste heat recycling assembly are integrally formed. The integral structure is adopted, so that the integral volume of the hydrogen production system is greatly reduced, and the integral weight of the system is lightened.
More specifically, the main structures of the system are connected through flange and welding connection technology, so that the whole system is integrated into a whole.
In another embodiment, the whole hydrogen production reactor is made of stainless steel, and the joint is sealed by adopting a welding process. Has the advantages of high temperature resistance, strong acid and alkali resistance, difficult deformation and long overall service life.
In another embodiment, as shown in fig. 5, an insulating layer 110 is provided on the outer side of the reaction chamber 1. The heat preservation layer 110 is heat preservation cotton, and heat loss is reduced by winding the heat preservation cotton on the outer side of the reaction box 1 for heat insulation.
In another embodiment, as shown in FIG. 1, the waste heat recycling assembly includes a plurality of recycling pipes 91, one end of the recycling pipe 91 is communicated with the flue gas outlet of the integrated hydrogen production reactor, and the other end is connected into the outer sleeve 23. The flue gas with combustible materials is circulated into the mixing area to be mixed with fuel, the mixed flue gas enters the combustion chamber 11 through the spray pipe 4 to be catalytically combusted, the flue gas after catalytic combustion is discharged through the external exhaust pipeline, and the external exhaust pipeline is arranged in the reaction cavity, so that the temperature in the flue gas after catalytic combustion is conveniently absorbed by the heat conducting medium.
Finally, it should be noted that: the foregoing description is only a preferred embodiment of the present invention, and the present invention is not limited thereto, but it is to be understood that modifications and equivalents of some of the technical features described in the foregoing embodiments may be made by those skilled in the art, although the present invention has been described in detail with reference to the foregoing embodiments. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. An integrated hydrogen production reactor, comprising:
A reaction box;
the fuel treatment assembly is arranged in the reaction box, and the air inlet end of the fuel treatment assembly extends out of the reaction box;
the separation plate is arranged in the reaction box and sleeved outside the fuel processing assembly, a combustion chamber is formed between the separation plate and the fuel processing assembly, and a reaction cavity is formed between the separation plate and the inner side wall of the reaction box;
The spray pipe is vertically arranged in the combustion chamber, one end of the spray pipe is communicated with the fuel processing assembly, and a plurality of spray holes of the spray pipe are arranged along the axial direction of the spray pipe;
a catalyst filled in the combustion chamber;
The vaporization superheater is arranged in the combustion chamber, and a feed inlet of the vaporization superheater is positioned outside the reaction box;
The reaction component is arranged in the reaction cavity, and the outlet of the vaporization superheater is communicated with the inlet of the reaction component;
A heat-conducting medium filled into the reaction chamber;
One end of the waste heat circulation assembly is communicated with a flue gas outlet of the integrated hydrogen production reactor, and the other end of the waste heat circulation assembly is connected to an air inlet of the fuel treatment assembly;
The fuel processing assembly includes:
An inner sleeve arranged in the reaction box;
The outer sleeve is sleeved outside the inner sleeve, a mixing area is formed between the outer sleeve and the inner sleeve, the air outlet end of the waste heat circulation assembly is connected into the outer sleeve, and the inlet of the spray pipe is connected into the mixing area;
one end of the fuel feed pipe extends into the inner sleeve and is communicated with the mixing area, and the other end of the fuel feed pipe is positioned outside the reaction tank;
The vaporization superheater includes
The first annular pipe is sleeved outside the fuel treatment assembly, and a raw material inlet is arranged on the first annular pipe;
the second annular pipe is sleeved outside the fuel treatment assembly, and a raw material outlet is arranged on the second annular pipe;
The inner coil pipe is sleeved outside the fuel treatment assembly, and two ends of the inner coil pipe are respectively communicated with the first annular pipe and the second annular pipe;
The outer coil pipe is sleeved outside the inner coil pipe, and two ends of the outer coil pipe are respectively communicated with the first annular pipe and the second annular pipe;
wherein the nozzle, when installed, is positioned between the inner coil and the outer coil.
2. The integrated hydrogen production reactor of claim 1 wherein the plurality of nozzles are uniformly disposed about the fuel processing assembly.
3. The integrated hydrogen production reactor according to claim 1 or 2, wherein when a plurality of nozzle holes are provided in a group along an axis direction of the nozzle pipe, the nozzle pipe is provided with a plurality of groups of the nozzle holes along a circumferential direction thereof.
4. The integrated hydrogen production reactor of claim 1, wherein the reaction assembly comprises:
The reaction tubes are arranged in the reaction cavity at equal intervals;
And one end of the air inlet pipe is communicated with the outlet of the vaporization superheater, and the other end of the air inlet pipe is connected into the reaction pipe.
5. The integrated hydrogen production reactor of claim 1, wherein the thermally conductive media is aluminum particles, copper particles, silver particles, or gold particles.
6. The integrated hydrogen production reactor of claim 1 wherein at least one auxiliary heating device is disposed within the combustion chamber.
7. The integrated hydrogen production reactor of claim 1, wherein the reaction tank, fuel processing assembly, divider plate, lance, vaporization superheater, reaction assembly, and waste heat recycling assembly are an integrated structure.
8. The integrated hydrogen production reactor of claim 1, wherein an insulating layer is provided on the outside of the reaction tank.
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| CN109592638A (en) * | 2018-12-29 | 2019-04-09 | 广东力行科创氢能有限公司 | A kind of self-heating device for producing hydrogen |
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| DE19639150C2 (en) * | 1996-09-24 | 1998-07-02 | Daimler Benz Ag | Central heating device for a gas generation system |
| DE19813053C2 (en) * | 1998-03-25 | 2001-10-18 | Xcellsis Gmbh | Reactor unit for a catalytic chemical reaction, especially for catalytic methanol reforming |
| DE19832386A1 (en) * | 1998-07-18 | 2000-01-27 | Dbb Fuel Cell Engines Gmbh | Reforming reactor with catalytic burner unit |
| CN112815316A (en) * | 2019-11-15 | 2021-05-18 | 中国科学院大连化学物理研究所 | Sleeve type catalytic combustor and application |
| CN111115577B (en) * | 2020-02-19 | 2024-09-17 | 李根钧 | Catalytic hydrogen production system and system for reducing nitrogen oxides by hydrogen combustion |
| CN213294670U (en) * | 2020-07-29 | 2021-05-28 | 四川蜀泰化工科技有限公司 | Catalytic heating coupling methanol hydrogen production system |
| CN112678770B (en) * | 2020-12-28 | 2022-11-29 | 四川天采科技有限责任公司 | Methanol and water hydrogen production device adopting PSA tail gas catalytic combustion for heat supply |
| CN115849302B (en) * | 2022-12-06 | 2024-08-09 | 中国船舶集团有限公司第七一一研究所 | Hydrogen production apparatus and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107327856A (en) * | 2017-05-25 | 2017-11-07 | 四川亚联高科技股份有限公司 | One kind catalysis combustion heat supplying system and heating technique |
| CN109592638A (en) * | 2018-12-29 | 2019-04-09 | 广东力行科创氢能有限公司 | A kind of self-heating device for producing hydrogen |
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