CN111115577A - Catalytic hydrogen production system and system for reducing nitrogen oxide by burning hydrogen - Google Patents
Catalytic hydrogen production system and system for reducing nitrogen oxide by burning hydrogen Download PDFInfo
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- CN111115577A CN111115577A CN202010101200.1A CN202010101200A CN111115577A CN 111115577 A CN111115577 A CN 111115577A CN 202010101200 A CN202010101200 A CN 202010101200A CN 111115577 A CN111115577 A CN 111115577A
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- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 291
- 239000001257 hydrogen Substances 0.000 title claims abstract description 209
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 209
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 121
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 121
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 96
- 239000002994 raw material Substances 0.000 claims abstract description 215
- 238000002485 combustion reaction Methods 0.000 claims abstract description 137
- 238000006243 chemical reaction Methods 0.000 claims abstract description 80
- 230000008016 vaporization Effects 0.000 claims abstract description 62
- 239000007789 gas Substances 0.000 claims abstract description 49
- 239000007788 liquid Substances 0.000 claims abstract description 49
- 239000003054 catalyst Substances 0.000 claims abstract description 45
- 238000009834 vaporization Methods 0.000 claims abstract description 41
- 238000000034 method Methods 0.000 claims abstract description 8
- 230000008569 process Effects 0.000 claims abstract description 7
- 238000002347 injection Methods 0.000 claims description 22
- 239000007924 injection Substances 0.000 claims description 22
- 238000010438 heat treatment Methods 0.000 claims description 18
- 239000000463 material Substances 0.000 claims description 15
- 239000010419 fine particle Substances 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 13
- 230000000087 stabilizing effect Effects 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 11
- 239000004020 conductor Substances 0.000 claims description 10
- 238000009423 ventilation Methods 0.000 claims description 9
- 238000009413 insulation Methods 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 7
- 238000000746 purification Methods 0.000 claims description 7
- 229910001369 Brass Inorganic materials 0.000 claims description 6
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 6
- 239000010951 brass Substances 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 6
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 6
- 239000000395 magnesium oxide Substances 0.000 claims description 6
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 6
- 229910052802 copper Inorganic materials 0.000 claims description 5
- 239000010949 copper Substances 0.000 claims description 5
- 229910052782 aluminium Inorganic materials 0.000 claims description 4
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 229910002804 graphite Inorganic materials 0.000 claims description 4
- 239000010439 graphite Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 36
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 238000001514 detection method Methods 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 9
- 239000000446 fuel Substances 0.000 description 9
- 230000009467 reduction Effects 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 229910001868 water Inorganic materials 0.000 description 6
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 5
- 229910001220 stainless steel Inorganic materials 0.000 description 5
- 239000010935 stainless steel Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 4
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 238000005485 electric heating Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 238000004321 preservation Methods 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 241000282414 Homo sapiens Species 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
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- 239000002737 fuel gas Substances 0.000 description 2
- 239000004519 grease Substances 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 230000006698 induction Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
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- 229910001873 dinitrogen Inorganic materials 0.000 description 1
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- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
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- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
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- 238000000926 separation method Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
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Images
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- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- 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
-
- 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
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
Abstract
The invention belongs to the technical field of hydrogen production, and particularly relates to a catalytic hydrogen production system and a system for reducing nitrogen oxide by hydrogen combustion. The catalytic hydrogen production system comprises a heat-insulating layer, and a raw material vaporization superheater, a raw material reaction temperature raising regulator and a catalytic reactor which are arranged in the heat-insulating layer and are sequentially connected; the raw material vaporization superheater is used for vaporizing the liquid hydrogen production raw material into hydrogen production raw material mixed gas; the raw material reaction temperature lifting regulator is used for lifting the temperature of the hydrogen production raw material mixed gas; the catalytic reactor is used for preparing hydrogen from the hydrogen production raw material mixed gas under the conditions of temperature and pressure required by the process through the catalytic action of the catalyst; high-temperature hydrogen generated by the catalytic reactor enters the raw material vaporization superheater and exchanges heat with the liquid hydrogen production raw material. The invention greatly reduces the reaction temperature in the hydrogen production process, saves energy, greatly improves the reaction rate, increases the hydrogen yield, and well controls the residual amount of hydrogen production raw materials which do not participate in the reaction.
Description
Technical Field
The invention belongs to the technical field of hydrogen production, and particularly relates to a catalytic hydrogen production system and a system for reducing nitrogen oxide by hydrogen combustion.
Background
At present, the scientific and technical level of China is greatly improved, social economy is rapidly developed, and the requirements of people on living environment are higher and higher, so that people have to pay high attention to environmental protection, and particularly, the better the more time in the aspects of environmental protection and energy conservation, the better the requirements are made, so that the traditional concept is changed, the functions of various combustion equipment are further improved, more combustion equipment which can ensure that various combustion equipment can be fully and cleanly combusted, the heat efficiency is high, and the combustion equipment provided with the ultra-clean smoke emission application system is very ideal.
Disclosure of Invention
In view of the above problems, the present invention provides a catalytic hydrogen production system and a system for reducing nitrogen oxide by burning hydrogen.
In order to achieve the purpose, the invention adopts the following technical scheme:
a catalytic hydrogen production system, comprising: the heat-preserving and heat-insulating layer is arranged in the heat-preserving and heat-insulating layer and is sequentially connected with the raw material vaporization superheater, the raw material reaction temperature raising regulator and the catalytic reactor; the raw material vaporizing superheater is used for vaporizing the liquid hydrogen production raw material into hydrogen production raw material mixed gas; the raw material reaction temperature lifting regulator is used for lifting the temperature of the hydrogen production raw material mixed gas and reaching the catalytic reaction temperature of the hydrogen production raw material mixed gas; the catalytic reactor is used for preparing hydrogen from the hydrogen-production raw material mixed gas under the conditions of temperature and pressure required by the process through the catalytic action of the catalyst;
and high-temperature hydrogen generated by the catalytic reactor enters the raw material vaporization superheater and exchanges heat with the liquid hydrogen production raw material to vaporize the liquid hydrogen production raw material at high temperature.
The raw material vaporization superheater comprises a raw material vaporization superheater shell and a plurality of raw material channels arranged in the raw material vaporization superheater shell, wherein the raw material channels are of tube bundle structures or plate structures and are communicated with the raw material reaction temperature lifting regulator;
and a high-temperature hydrogen inlet and a high-temperature hydrogen outlet are formed in the shell of the raw material vaporization superheater, and the high-temperature hydrogen inlet is communicated with the catalytic reactor.
The raw material reaction temperature lifting adjuster comprises a raw material reaction temperature self-control adjusting heater, a raw material reaction temperature lifting adjuster heat conduction material and a raw material reaction temperature lifting adjuster heated tube, wherein one or more raw material reaction temperature lifting adjuster heated tubes are arranged in the raw material reaction temperature self-control adjusting heater; the heated pipe of the raw material reaction temperature raising regulator is a straight pipe or a curve pipe, and two ends of the heated pipe are respectively communicated with the raw material vaporization superheater and the catalytic reactor.
The catalytic reactor comprises a catalytic reactor constant-temperature regulating heater, a catalytic reactor heat conducting material and a catalyst containing pipe, wherein one or more catalyst containing pipes are arranged in the catalytic reactor constant-temperature regulating heater; the catalyst containing pipe is a straight pipe or a curve pipe, one end of the catalyst containing pipe is connected with the heated pipe of the raw material reaction temperature raising regulator through a communicating pipeline, and the other end of the catalyst containing pipe is connected with the raw material vaporization superheater.
The raw material reaction temperature raising adjuster heat conduction material and the catalytic reactor heat conduction material are both made of heat conduction powder or heat conduction fine particles made of red copper, brass, magnesium oxide, aluminum or heat conduction graphite.
The catalytic hydrogen production system also comprises a raw material auxiliary heating and vaporizing device and a raw material quantitative control conveyor, wherein the raw material auxiliary heating and vaporizing device is connected between the raw material vaporizing superheater and the raw material quantitative control conveyor; the raw material quantitative control conveyor is used for quantitatively conveying hydrogen production raw materials; the raw material auxiliary heating and vaporizing device is used for heating and vaporizing the liquid hydrogen production raw material when the catalytic hydrogen production system is firstly cold started, and the catalytic hydrogen production system is closed after normal work.
The catalytic hydrogen production system also comprises a gas-liquid separator, a hydrogen gas condenser and a hydrogen gas purification processor which are connected in sequence, wherein the gas-liquid separator is communicated with the high-temperature hydrogen in the raw material vaporization superheater; the bottom of the raw material vaporization superheater is connected with the bottom of the gas-liquid separator through a condensate discharge valve, and the bottom of the gas-liquid separator is provided with a raw material liquid discharge port for discharging unreacted liquid hydrogen production raw materials.
A system for reducing nitrogen oxides by hydrogen combustion, comprising a combustion device, a hydrogen burner and the catalytic hydrogen production system as claimed in any one of claims 1 to 7, wherein the combustion device comprises a main combustion chamber and a discharge flue arranged at the upper part of the main combustion chamber; the catalytic hydrogen production system sprays ignited hydrogen to the upper part of the combustion chamber and/or the discharge flue through the hydrogen combustor, and the burning hydrogen reduces nitrogen oxides contained in the flue gas at the upper part of the combustion chamber and/or the discharge flue.
The hydrogen combustor comprises an outer sleeve, an ignition assembly, a central fuel gas inlet pipeline, a hydrogen gas injection burner tip, a burner head and a flame stabilizing combustion disc, wherein the side wall of the outer sleeve is of a hollow structure, and a cooling medium is filled in the outer sleeve; a central gas inlet pipeline and a plurality of hydrogen gas inlet pipelines surrounding the periphery of the central gas inlet pipeline are arranged in the outer sleeve; the flame stabilizing combustion disc is arranged at the end part of the outer sleeve, and a combustion head, a plurality of hydrogen injection combustion nozzles distributed around the combustion head and a plurality of rotational flow ventilation holes are arranged on the flame stabilizing combustion disc; the combustion head is connected with the central gas inlet pipeline and is used for igniting hydrogen; each hydrogen injection burner is respectively connected with each hydrogen inlet pipeline;
the ignition assembly is arranged on one side of the combustion head and used for igniting gas sprayed out of the combustion head.
The outer circumference of the flame stabilizing combustion disc is provided with a plurality of rotational flow guide grooves, and the end surface of the flame stabilizing combustion disc is provided with at least one group of rotational flow vent holes which are uniformly distributed along the circumferential direction; the cyclone ventilation holes are obliquely arranged, and wind led out from the cyclone ventilation holes and the cyclone guide grooves rises spirally and is fully mixed with nitrogen oxides in hydrogen and flue gas.
The side wall of the discharge flue is of a water-cooled wall type structure, and a water-cooled pipe is arranged in the discharge flue.
The invention has the advantages and beneficial effects that:
1. the invention utilizes the hydrogen production raw material and the catalytic hydrogen production system, and simultaneously cooperates with the application of the hydrogen production catalyst under the guarantee of the factors such as temperature, pressure, feeding quantity and the like, so that the reaction temperature is greatly reduced, the energy is saved, the activation energy in the reaction is also reduced, the reaction rate is greatly improved, the hydrogen production quantity is increased, the residual quantity of the hydrogen production raw material which does not participate in the reaction is well controlled, and the residual raw material can be reused.
2. The invention can utilize the cooperation of the waste heat of the combustion equipment and the normal heat energy, accurately fix the temperature, react methanol and methanol water under the catalytic action of the catalyst to prepare hydrogen gas, which is used for the combustion of the combustion equipment, namely, the heat energy is increased, and the hydrogen gas can also be used as a reducing agent for reducing nitrogen oxides, so that the prior urea or various ammonia materials used for the traditional flue gas denitration are changed, a large amount of funds are saved for the denitration process, and the nitrogen oxides can be reduced by adopting the hydrogen gas to burn, namely, the combustion heat energy can be increased for the combustion equipment, and the denitration can be realized by killing two birds.
3. The invention can also collect and utilize the high-temperature steam discharged after the high-temperature steam of the thermal power plant completes work (after the steam turbine is pushed to complete work), can be directly used as one of reaction raw materials, saves a large amount of capital for resource consumption, and can also utilize the heat energy of the part of the steam to heat and exchange the raw materials so as to save conventional energy.
Drawings
FIG. 1 is a schematic diagram of a catalytic hydrogen production system according to the present invention;
FIG. 2 is a schematic diagram of the hydrogen combustion nitrogen oxide reduction system of the present invention;
FIG. 3 is a schematic view showing the construction of a hydrogen burner according to the present invention;
fig. 4 is a right side view of fig. 3.
In the figure: 1. a methanol water or water vapor raw material inlet, a methanol deionized water mixed liquid raw material inlet, a methanol water or water vapor mixed liquid raw material inlet, a methanol deionized water mixed liquid raw material inlet, a refined methanol raw material inlet, a raw material quantitative control conveyor, a system control raw material allowance overflow return valve, a raw material auxiliary heating vaporization device, a raw material vaporization superheater, a catalytic reactor constant temperature regulation heater, a catalytic reactor heat conduction material, a catalyst containing pipe, a catalytic reactor, a raw material reaction temperature lifting regulator heat conduction material, a raw material reaction temperature self-control regulation heater, a raw material reaction temperature lifting regulator heating pipe, a raw material reaction temperature lifting regulator, a connecting pipeline, a heat preservation and heat insulation layer, a hydrogen gas combustion anti-backfire safety protection device, a combustion equipment upper hydrogen gas conveying pipeline, a main combustion chamber upper combustion control valve, 21. a discharge flue hydrogen gas control valve, 22, a discharge flue gas burner in the discharge flue, 23, a combustion area hydrogen gas conveying pipeline, 24, a hydrogen gas purification processor, 25, a main combustion chamber upper hydrogen gas burner, 26, a flue gas discharge direction after combustion reaction of the combustion equipment main combustion chamber, 27, nitrogen oxide combustion reduction areas II, 28, nitrogen oxide combustion reduction areas I, 29, a hydrogen gas condenser, 30, a combustion area hydrogen gas conveying pipeline control valve, 31, a combustion area hydrogen gas burner, 32, a combustion area, 33, the main combustion chamber, 34, a gas-liquid separator, 35, a raw material liquid discharge port, 36, a condensate discharge valve, 37, a high-voltage transmission wire, 38, a central gas inlet pipeline, 39, a flame temperature detection signal feedback wire, 40, a middle ring hydrogen gas inlet pipeline, 41, an outer ring gas inlet pipeline, 42 and a cooling medium, 43. the device comprises an outer sleeve, 44, an outer ring hydrogen injection burner, 45, a middle ring hydrogen injection burner, 46, a flame temperature detection induction needle, 47, a combustion head, 48, a high-pressure discharge ignition needle, 49, a flame stabilizing combustion disc, 50, a cyclone guide groove, 51 and an outer ring cyclone vent hole, 52 is a middle ring cyclone vent hole, and 53 is flame combusted by the combustion head.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in detail with reference to the accompanying drawings and specific embodiments.
Example one
As shown in fig. 1, the present invention provides a catalytic hydrogen production system comprising: a heat insulation layer 17, and a raw material vaporization superheater 7, a raw material reaction temperature raising regulator 15 and a catalytic reactor 11 which are arranged in the heat insulation layer 17 and are sequentially connected; the raw material vaporizing superheater 7 is used for vaporizing the liquid hydrogen production raw material into hydrogen production raw material mixed gas; the raw material reaction temperature raising adjuster 15 is used for raising the temperature of the hydrogen production raw material mixed gas and reaching the catalytic reaction temperature of the hydrogen production raw material mixed gas; the catalytic reactor 11 is used for preparing hydrogen from the hydrogen production raw material mixed gas under the conditions of temperature and pressure required by the process through the catalytic action of a catalyst; the high-temperature hydrogen generated by the catalytic reactor 11 enters the raw material vaporizing superheater 7 and exchanges heat with the liquid hydrogen production raw material, so that the liquid hydrogen production raw material is vaporized at high temperature.
The raw material vaporization superheater 7 comprises a raw material vaporization superheater shell and a plurality of raw material channels arranged in the raw material vaporization superheater shell, wherein the raw material channels are of tube bundle structures or plate structures and are communicated with a raw material reaction temperature lifting regulator 15; the shell of the raw material vaporization superheater is provided with a high-temperature hydrogen inlet and a high-temperature hydrogen outlet, and the high-temperature hydrogen inlet is communicated with the catalytic reactor 11.
The raw material reaction temperature raising adjuster 15 comprises a raw material reaction temperature self-control adjusting heater 13, a raw material reaction temperature raising adjuster heat conduction material 12 and a raw material reaction temperature raising adjuster heated tube 14, wherein one or more raw material reaction temperature raising adjuster heated tubes 14 which are uniformly arranged are arranged in the raw material reaction temperature self-control adjusting heater 13, and the raw material reaction temperature raising adjuster heat conduction material 12 is filled between the raw material reaction temperature self-control adjusting heater 13 and the raw material reaction temperature raising adjuster heated tube 14; the heated tube 14 of the raw material reaction temperature raising regulator is a straight tube or a curved tube, and two ends of the heated tube are respectively communicated with the raw material channel of the raw material vaporization superheater 7 and the catalytic reactor 11.
In the embodiment of the present invention, the outer layer of the raw material reaction temperature raising adjuster 15 is a raw material reaction temperature self-control adjusting heater 13, and the raw material reaction temperature self-control adjusting heater 13 includes an electric heating coil heater, an electric heating plate heater, a crawler-type ceramic high-temperature heater or an electromagnetic high-temperature adjusting heater, etc. The raw material reaction temperature raising adjuster heat conductive material 12 is a heat conductive powder, for example: red copper powder, brass powder, magnesium oxide powder, aluminum powder or heat conducting graphite powder and the like; or the raw material reaction temperature raising regulator heat conduction material 12 is heat conduction fine particles, such as: red copper fine particles, brass fine particles, magnesium oxide fine particles, aluminum fine particles, or heat conductive graphite fine particles; at low temperature, the heat conduction oil can also be adopted as the heat conduction material 12 of the raw material reaction temperature raising regulator; or the heat conduction material 12 of the raw material reaction temperature raising regulator adopts high-temperature heat conduction oil, high-temperature dry steam (water vapor) or high-temperature air and the like. The heated tube 14 of the raw material reaction temperature raising regulator is a high temperature resistant stainless steel tube, and the shape of the heated tube is made into a spiral tube type or a continuous S-shaped tube type structure.
The catalytic reactor 11 comprises a catalytic reactor constant temperature regulating heater 8, a catalytic reactor heat conducting material 9 and a catalyst containing pipe 10, wherein one or more catalyst containing pipes 10 which are uniformly arranged are arranged in the catalytic reactor constant temperature regulating heater 8, and the catalytic reactor heat conducting material 9 is filled between the catalytic reactor constant temperature regulating heater 8 and the catalyst containing pipe 10; the catalyst containing pipe 10 is a straight pipe or a curved pipe, and one end thereof is connected to the heated pipe 14 of the raw material reaction temperature raising regulator through a communication pipe 16, and the other end thereof is connected to a high-temperature hydrogen inlet of the raw material vaporization superheater 7.
In the embodiment of the invention, the outer layer of the catalytic reactor 11 is the catalytic reactor constant temperature regulating heater 8, and the catalytic reactor constant temperature regulating heater 8 comprises an electric heating coil heater, an electric heating plate heater, a crawler-type ceramic high temperature heater or an electromagnetic high temperature regulating heater and the like. The catalytic reactor thermally conductive material 9 is a thermally conductive powder such as: red copper powder, brass powder, magnesium oxide powder, aluminum powder or heat conducting graphite powder and the like; or the catalytic reactor thermally conductive material 9 is thermally conductive fine particles such as: red copper fine particles, brass fine particles, magnesium oxide fine particles, aluminum fine particles, or heat conductive graphite fine particles. Heat conducting oil is used at medium and low temperature.
In the embodiment of the present invention, the catalyst-containing tube 10 is a straight stainless steel tube or a continuous S-shaped bent tube. After the hydrogen production catalyst is filled in the pipe, the pipe heads at two ends are 10-50 mm higher than the sealing plates at two ends, holes (air inlet or outlet holes smaller than the particle size of the catalyst) are drilled on the pipe heads, meanwhile, sealing covers at two ends (preventing the catalyst from flowing out) are arranged or welded, and air inlet or outlet holes (holes smaller than the particle size of the catalyst) are drilled on the sealing covers at two ends.
In the embodiment of the invention, the heat insulation layer 17 comprises a metal shell and a high-temperature-resistant heat insulation material arranged in the metal shell, wherein the metal shell is made of a stainless steel plate or a paint iron plate and the like; the high-temperature resistant heat-insulating material adopts rock wool fiber felt, aluminum silicate fiber felt or light heat-insulating particles and the like.
In the embodiment of the invention, the catalytic hydrogen production system further comprises a raw material auxiliary heating and vaporizing device 6 and a raw material quantitative control conveyor 4, wherein the raw material auxiliary heating and vaporizing device 6 is connected between the raw material vaporization superheater 7 and the raw material quantitative control conveyor 4; the raw material quantitative control conveyor 4 is used for quantitatively conveying hydrogen production raw materials and is provided with a methanol water or water vapor raw material inlet 1, a methanol deionized water mixed liquid raw material inlet 2 and a refined methanol raw material inlet 3; the top of the raw material quantitative control conveyor 4 is provided with a system control raw material allowance overflow return valve 5. The raw material auxiliary heating and vaporizing device 6 is used for heating and vaporizing the liquid hydrogen production raw material when the catalytic hydrogen production system is firstly cold started, and is closed after the catalytic hydrogen production system normally works.
In the embodiment of the invention, the raw material auxiliary heating and vaporizing device 6 is a commercially available product and adopts a micro steam generator provided by Shanghai Ji Yi Heat energy Equipment Co. The raw material quantitative control conveyor 4 adopts a quantitative conveying pump.
In the embodiment of the invention, the catalytic hydrogen production system further comprises a gas-liquid separator 34, a hydrogen gas condenser 29 and a hydrogen gas purification processor 24 which are connected in sequence, wherein the gas-liquid separator 34 is communicated with the high-temperature hydrogen in the raw material vaporization superheater 7; the bottoms of the raw material vaporization superheater 7 and the gas-liquid separator 34 are connected by a condensate discharge valve 36, the bottom of the gas-liquid separator 34 is provided with a raw material liquid discharge port 35, and the raw material liquid discharge port 35 is used for discharging unreacted liquid hydrogen production raw material.
In the embodiment of the invention, three groups of hydrogen production raw materials and three hydrogen production catalysts are included, and the three hydrogen production catalysts are respectively used in three temperature sections, namely a low-temperature section: 150-200 ℃ and medium temperature: 200-300 ℃ and high-temperature section: 300-500 ℃. In the embodiment of the invention, the three hydrogen production catalysts are commercial products, and the high-temperature hydrogen production catalyst is a nickel-based multi-component combined metal catalyst; the medium-temperature hydrogen production catalyst is a copper-based multi-element combined metal catalyst; the low-temperature hydrogen production catalyst is a noble metal and rare earth combined multi-element catalyst.
Three groups of hydrogen production raw materials are respectively selected according to different geographical environments and different using modes required by hydrogen production, the three groups of hydrogen production raw materials are respectively refined methanol (with the purity of 99 percent), refined methanol and deionized water are prepared into mixed liquor according to the proportion of 1:1, the refined methanol and water vapor have the same mass (weight) according to the proportion of 1:1, and the three groups of hydrogen production raw materials are respectively conveyed through three groups of pipes and respectively fed and mixed in a catalytic hydrogen production system to be used as raw materials for preparing hydrogen gas (one group of raw materials is selected for hydrogen production according to actual needs).
The three groups of hydrogen production raw materials can reach the operation pressure set by the system when the temperature is raised to the reaction temperature, the operation pressure is generally determined according to the unit hour hydrogen production amount of the catalytic hydrogen production system, the operation pressure determined in the embodiment is 0.3 MPa-3 MPa, the feeding flow velocity (liquid space velocity) of the three groups of raw materials is determined according to the hydrogen production amount which can be completed after the catalytic hydrogen production system passes through the hydrogen production catalyst bed layer per hour, and the feeding flow velocity is 0.1-3 h < -1 > which is the counting range of the liquid air velocity specified by the catalytic hydrogen production system.
The three groups of hydrogen production raw materials can prepare hydrogen gas when the conditions such as reaction temperature, operation pressure, liquid space velocity, catalyst catalysis and the like are all met, and the chemical reaction formula is as follows:
the general formula is as follows: CH (CH)30H+H20＝C02+3H2-49.5KJ/mol
The method comprises the following steps: 1. CH (CH)30H＝C0+2H2-90.7KJ/mol
2、C0+H20＝C02+H2+41.19KJ/mol
Wherein, this application system chooses for use three kinds of hydrogen manufacturing catalysts respectively according to different hydrogen manufacturing environment and various advantage conditions that can provide in addition, respectively: the low-temperature hydrogen production catalyst has the use temperature range of 150-200 ℃. The medium-temperature hydrogen production catalyst has the use temperature range of 200-300 ℃. The high-temperature hydrogen production catalyst has the use temperature range of 300-500 ℃.
The working process of the invention is as follows:
one group of hydrogen production raw materials are selected according to actual needs, the determined group of hydrogen production raw materials are conveyed into a raw material quantitative control conveyor 4 through a pipeline, the hydrogen production raw material inlet amount is accurately controlled by the raw material quantitative control conveyor 4, meanwhile, redundant raw materials are conveyed back to a place where the raw materials are stored through a system control surplus overflow return valve 5, the quantified raw materials enter a raw material auxiliary heating and vaporizing device 6, the device is only used when the catalytic hydrogen production system starts to work, after the system normally runs and high-temperature hydrogen gas is produced, the raw material auxiliary heating function is immediately closed, the system overpressure safety interlock function normally works), and the raw materials are conveyed into a raw material vaporization superheater 7 after being vaporized at high temperature. Then, the vaporized and superheated hydrogen production raw material is conveyed to a raw material reaction temperature raising regulator 15, heated to a required reaction temperature, and then conveyed into a catalyst containing pipe 10 in the catalytic reactor 11 through a communication pipeline 16 between the catalytic reactor 11 and the raw material reaction temperature raising regulator 15 to perform a methanol decomposition reaction and a carbon monoxide-steam shift reaction to generate a high-temperature mixed gas (a mixed gas rich in hydrogen) such as hydrogen and carbon dioxide, and the high-temperature mixed gas after the reaction leaves the catalytic reactor 11 and then enters a raw material vaporization superheater 7. The high-temperature mixed gas after the reaction is cooled greatly by cooling and heat exchange (heat exchange, vaporization and overheating of the hydrogen production raw material) for a certain time in the space, and then enters a gas-liquid separator 34 for gas-liquid separation treatment. In addition, when the system is designed, a small part of high-temperature mixed gas after reaction is considered, and condensate generated after the system stops working enters the gas-liquid separator 34 through the condensate discharge valve 36, and the unreacted raw material liquid cooled and separated by the gas-liquid separator 34 is discharged through the raw material liquid discharge port 35 and returned to the place where the raw material is stored. The separated hydrogen gas enters a hydrogen gas condenser 29, is condensed and cooled, then enters a hydrogen gas purification processor 24 for purification treatment, so that the prepared hydrogen gas has certain use purity and requirements, and then is conveyed through a pipeline, so that the prepared hydrogen gas is practically applied.
The range of hydrogen gas use is: the first is used for hydrogenation of protective gas, hydrogen fuel cell, high energy gas fuel and grease; the second is used for burning and reducing the nitrogen oxide, because various fuels used by large and medium-sized burning equipment are mainly used for supporting combustion by air in the burning process in a burning chamber, the nitrogen in the air is oxidized into nitrogen oxide gas at high temperature, the nitrogen oxide is harmful gas, and the nitrogen oxide can be reduced into nitrogen and water by burning hydrogen gas in order to remove the nitrogen hydride.
In conclusion, the hydrogen gas prepared by the catalytic hydrogen production system is applied to the fields of chemical gas protection, hydrogen fuel cells, special high-energy gas fuel, powder metallurgy, industrial metal heat treatment, bioengineering, electronic industry, glass industry, reduction treatment of nitrogen oxides generated by grease hydrogenation and high-temperature combustion and the like.
Example two
As shown in fig. 2, the system for reducing nitrogen oxide by hydrogen combustion provided by the present invention includes a combustion device, a hydrogen burner, and a catalytic hydrogen production system as provided in any of the above embodiments, wherein the catalytic hydrogen production system injects ignited hydrogen into an upper portion (also called a tail portion) of a combustion chamber of the combustion device and/or a flue through the hydrogen burner, and the burned hydrogen reduces nitrogen oxide in flue gas at the upper portion of the combustion chamber and/or in the flue.
After the hydrogen produced by the catalytic hydrogen production system is purified by the hydrogen gas purification processor 24, the pure hydrogen gas is delivered into the hydrogen gas combustion anti-backfire security device 18, so that the hydrogen gas can be safely applied to conventional combustion and reduction of nitrogen oxides in flue gas.
As shown in figure 2, the combustion equipment comprises a main combustion chamber 33 and a discharge flue arranged on the upper part of the main combustion chamber 33, wherein the lower part of the main combustion chamber 33 is a combustion area 32, the upper part of the main combustion chamber 33 is a nitrogen oxide combustion reduction area I28, the inner cavity of the discharge flue is a nitrogen oxide combustion reduction area II 27, the side wall of the discharge flue is of a water-cooled wall type structure, a water-cooled pipe is arranged in the discharge flue, the water-cooled wall of the discharge flue and the water-cooled pipe are communicated with the water-cooled wall pipe of the combustion equipment, and the water in the water-cooled wall of the discharge flue and the water-cooled pipe inside the discharge.
The hydrogen gas produced by the catalytic hydrogen production system is distributed into two pipelines for conveying, namely a hydrogen gas conveying pipeline 19 on the upper part of the combustion equipment and a hydrogen gas conveying pipeline 23 in a combustion area. The upper hydrogen gas conveying pipeline 19 of the combustion device sprays hydrogen gas into the upper part of the main combustion chamber 33 and the discharge flue through the upper hydrogen burner 25 of the main combustion chamber and the hydrogen burner 22 in the discharge flue respectively. The upper hydrogen gas conveying pipeline 19 of the combustion equipment is provided with a main combustion chamber upper hydrogen gas combustion control valve 20 and a discharge flue hydrogen gas control valve 21, wherein the main combustion chamber upper hydrogen gas combustion control valve 20 is used for controlling the hydrogen gas entering the upper part of the main combustion chamber 33, and the discharge flue hydrogen gas control valve 21 is used for controlling the hydrogen gas entering the discharge flue. The combustion zone hydrogen gas conveying pipeline 23 sprays hydrogen gas into the combustion zone 32 through a plurality of combustion zone hydrogen gas combustors 31, and a combustion zone hydrogen gas conveying pipeline control valve 30 is arranged on the combustion zone hydrogen gas conveying pipeline 23.
Injecting hydrogen gas into the combustion zone 32 for conventional fuel combustion; hydrogen gas is injected into the upper part of the main combustion chamber 33 and the exhaust flue for combustion reduction of nitrogen oxides. As various fuels used by large and medium-sized combustion equipment are mainly used for supporting combustion by using air in the combustion process in a combustion chamber, nitrogen in the air is oxidized into nitrogen oxide gas at high temperature, and the nitrogen oxide is harmful gas. To remove nitrogen hydrides, nitrogen oxides can be reduced to nitrogen gas and carbon dioxide by mixing hydrogen gas and carbon monoxide gas with nitrogen oxides and then burning the mixture.
The chemical reaction formula for reducing nitrogen oxides by hydrogen combustion is as follows:
the chemical reaction formula for reducing nitrogen oxides by burning carbon monoxide gas is as follows:
as shown in fig. 3-4, the hydrogen burner comprises an outer casing 43, an ignition assembly, a central fuel gas inlet pipe 38, a hydrogen gas inlet pipe, a hydrogen gas injection burner, a burner head 47 and a flame-stabilizing burner disk 49, wherein the side wall of the outer casing 43 is a hollow structure, and a cooling medium 42 is filled in the side wall; a central gas inlet pipeline 38 and a plurality of hydrogen gas inlet pipelines surrounding the central gas inlet pipeline 38 are arranged in the outer sleeve 43; the flame stabilizing combustion disc 49 is arranged at the end part of the outer sleeve 43, and the flame stabilizing combustion disc 49 is provided with a combustion head 47, a plurality of hydrogen injection combustion nozzles and a plurality of cyclone ventilation holes which are distributed around the combustion head 47; the burner head 47 is connected to the central gas inlet conduit 38 for igniting the hydrogen; each hydrogen injection burner is respectively connected with each hydrogen inlet pipeline; the ignition assembly is disposed at one side of the burner head 47 and is used for igniting the gas sprayed from the burner head 47.
The ignition assembly comprises a high-voltage power transmission lead 37, a flame temperature detection signal feedback lead 39, a flame temperature detection sensing needle 46 and a high-voltage discharge ignition needle 48, wherein the flame temperature detection sensing needle 46 and the high-voltage discharge ignition needle 48 are arranged on a flame stabilizing combustion disc 49, the high-voltage power transmission lead 37 is connected with the high-voltage discharge ignition needle 48, and the flame temperature detection signal feedback lead 39 is connected with the flame temperature detection sensing needle 46. The task of returning the detection signal of the flame temperature detection sensing needle 46 is returned to the control terminal of the application system by the flame temperature detection signal feedback wire 39, so that the operation safety of the application system and the combustion equipment is ensured.
In the embodiment of the present invention, the hydrogen injection burner includes a plurality of circumferentially distributed middle ring hydrogen injection burners 45 and a plurality of circumferentially distributed outer ring hydrogen injection burners 44; the hydrogen gas inlet pipeline comprises a plurality of middle ring hydrogen gas inlet pipelines 40 and a plurality of outer ring hydrogen gas inlet pipelines 41, wherein the plurality of middle ring hydrogen gas inlet pipelines 40 are respectively connected with each middle ring hydrogen gas injection burner tip 45; the plurality of outer ring hydrogen gas intake pipes 41 are connected to the outer ring hydrogen gas injection burners 44, respectively.
As shown in fig. 4, a plurality of swirl guide grooves 50 are formed on the outer circumference of the flame holding combustion disc 49, and at least one set of swirl vent holes uniformly distributed along the circumferential direction are formed on the end surface of the flame holding combustion disc 49; the cyclone ventilation holes are obliquely arranged, and wind led out by the cyclone ventilation holes and the cyclone guide grooves 50 rises spirally and is fully mixed with nitrogen oxides in the hydrogen and the flue gas. The middle ring hydrogen gas injection burner 45 and the outer ring hydrogen gas injection burner 44 are supplied with hydrogen gas by the middle ring hydrogen gas inlet pipe 40 and the outer ring hydrogen gas inlet pipe 41 respectively for injection combustion.
In the embodiment of the present invention, the flame holding combustion disk 49 is provided with the middle ring swirl vent hole 52 and the outer ring swirl vent hole 51, wherein the middle ring swirl vent hole 52 is provided between the middle ring hydrogen injection burner 45 and the outer ring hydrogen injection burner 44, and the outer ring swirl vent hole 51 is provided outside the outer ring hydrogen injection burner 44.
In the embodiment of the present invention, the outer casing 43 is made of a high temperature resistant material, the material includes high temperature resistant stainless steel or high temperature impact resistant ceramic, and the cooling medium includes cooling water or high pressure high speed cooling air. The flame holding combustion disk 49 is made of high temperature resistant stainless steel or high temperature resistant impact series ceramics, the outer diameter of the flame holding combustion disk 49 is provided with a rotational flow guide groove 50 which forms a certain angle and depth with the axis, the end surface of the flame holding combustion disk is drilled with a hydrogen gas jet combustion nozzle through hole and a rotational flow vent hole which forms a certain angle with the axis, and the end surface of the flame holding combustion disk 49 is provided with a high-pressure discharge ignition needle 48, a flame temperature detection induction needle 46, a combustion head 47 and the like. The flame holding combustion disk 49 provides a strong air intake swirl by providing the swirl guide groove 50 and the swirl vent holes, thereby improving the stability of hydrogen combustion. In order to eliminate the influence of high-temperature hot corrosion and high-temperature heat conduction on the normal operation of the special burner for hydrogen gas, the special burner is cooled by the cooling medium 42 in the outer sleeve 43.
In the embodiment of the invention, the hydrogen gas combustion anti-backfire security device 18 is a commercially available product, which is purchased from Zhejiang Xuan valve Limited company and has the model number of DN 15. The hydrogen gas combustion anti-backfire security device 18 comprises a plurality of hydrogen gas backfire flame arresters connected in parallel, a multi-channel electric control hydrogen valve island (combined electromagnetic valve) and the like. The hydrogen gas combustion anti-backfire security device 18 is used for preventing the backfire phenomenon caused by the fact that the flow velocity of hydrogen gas is less than the combustion velocity of hydrogen gas in the combustion process of hydrogen gas, so a hydrogen gas flame arrester must be installed. In addition, the multi-channel electric control hydrogen valve island is designed and installed to be convenient for controlling the safe use of the hydrogen burner on the multi-channel pipeline, and the valve island respectively controls the closing of the hydrogen pipeline to provide no hydrogen if a flame temperature sensing needle on a flame stabilizing disc of the hydrogen burner does not detect the temperature generated by the combustion of a gas combustion head.
The invention utilizes hydrogen production raw materials (methanol and water, or methanol and water vapor) in a catalytic hydrogen production system, and simultaneously cooperates with the application of the hydrogen production catalyst under the guarantee of factors such as temperature, pressure, feeding amount and the like, so that the reaction temperature is greatly reduced, the energy is saved, the activation energy in the reaction is also reduced, the reaction rate is greatly improved, the hydrogen production amount is increased, the residual amount of the hydrogen production raw materials which do not participate in the reaction is well controlled, and the residual raw materials can be reused.
The catalytic hydrogen production system using methanol water as a raw material adopts overall heat preservation and insulation treatment (except devices which need to be cooled, condensed and combust to reduce nitrogen oxide parts respectively), and adopts overall heat preservation and insulation packaging measures so as to reduce energy consumption, improve the utilization rate of waste heat recovery, facilitate the control of the overall reaction temperature of the catalytic hydrogen production system, prolong the service life of a hydrogen production catalyst and increase the hydrogen production of the system.
The system for reducing nitrogen oxide by burning hydrogen can be fused in any equipment using various fuels for burning, can be independently used as conventional gas fuel for burning, and can be used as a reducing agent for reducing harmful gas nitrogen oxide, and can be well reduced into nitrogen and water for emission no matter how much the content of the harmful gas nitrogen oxide in flue gas is, so that the harm of pollutants to human beings is avoided, and the human life in a good green environment is ensured.
The above description is only an embodiment of the present invention, and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, improvement, extension, etc. made within the spirit and principle of the present invention are included in the protection scope of the present invention.
Claims (11)
1. A catalytic hydrogen production system, comprising: a heat insulation layer (17), and a raw material vaporization superheater (7), a raw material reaction temperature raising regulator (15) and a catalytic reactor (11) which are arranged in the heat insulation layer (17) and are sequentially connected; the raw material vaporizing superheater (7) is used for vaporizing the liquid hydrogen production raw material into hydrogen production raw material mixed gas; the raw material reaction temperature lifting regulator (15) is used for lifting the temperature of the hydrogen production raw material mixed gas and reaching the catalytic reaction temperature of the hydrogen production raw material mixed gas; the catalytic reactor (11) is used for preparing hydrogen from the hydrogen-production raw material mixed gas under the conditions of temperature and pressure required by the process through the catalytic action of a catalyst;
high-temperature hydrogen generated by the catalytic reactor (11) enters the raw material vaporization superheater (7) and exchanges heat with the liquid hydrogen production raw material to vaporize the liquid hydrogen production raw material at high temperature.
2. The system for catalytic hydrogen production according to claim 1, wherein the raw material vaporization superheater (7) comprises a raw material vaporization superheater shell and a plurality of raw material channels arranged in the raw material vaporization superheater shell, and the raw material channels are of a tube bundle structure or a plate structure and are communicated with the raw material reaction temperature raising regulator (15);
and a high-temperature hydrogen inlet and a high-temperature hydrogen outlet are formed in the shell of the raw material vaporization superheater, and the high-temperature hydrogen inlet is communicated with the catalytic reactor (11).
3. The catalytic hydrogen production system according to claim 1, wherein the raw material reaction temperature raising regulator (15) comprises a raw material reaction temperature self-control regulating heater (13), a raw material reaction temperature raising regulator heat-conducting material (12) and a raw material reaction temperature raising regulator heated tube (14), wherein one or more raw material reaction temperature raising regulator heated tubes (14) are arranged in the raw material reaction temperature self-control regulating heater (13), and the raw material reaction temperature raising regulator heat-conducting material (12) is filled between the raw material reaction temperature self-control regulating heater (13) and the raw material reaction temperature raising regulator heated tube (14); the heated tube (14) of the raw material reaction temperature raising regulator is a straight tube or a curve tube, and two ends of the heated tube are respectively communicated with the raw material vaporization superheater (7) and the catalytic reactor (11).
4. The catalytic hydrogen production system according to claim 3, wherein the catalytic reactor (11) comprises a catalytic reactor thermostatic regulating heater (8), a catalytic reactor heat conducting material (9) and a catalyst containing pipe (10), wherein one or more catalyst containing pipes (10) are arranged in the catalytic reactor thermostatic regulating heater (8), and the catalytic reactor heat conducting material (9) is filled between the catalytic reactor thermostatic regulating heater (8) and the catalyst containing pipes (10); the catalyst containing pipe (10) is a straight pipe or a curve pipe, one end of the catalyst containing pipe is connected with the heated pipe (14) of the raw material reaction temperature raising regulator through a communicating pipeline (16), and the other end of the catalyst containing pipe is connected with the raw material vaporization superheater (7).
5. A catalytic hydrogen production system according to claim 4, characterized in that the raw material reaction temperature raising regulator heat conduction material (12) and the catalytic reactor heat conduction material (9) both use heat conduction powder or heat conduction fine particles made of red copper, brass, magnesium oxide, aluminum or heat conduction graphite.
6. The catalytic hydrogen production system according to claim 1, further comprising a raw material auxiliary heating vaporization device (6) and a raw material quantitative control conveyor (4), wherein the raw material auxiliary heating vaporization device (6) is connected between the raw material vaporization superheater (7) and the raw material quantitative control conveyor (4); the raw material quantitative control conveyor (4) is used for quantitatively conveying hydrogen production raw materials; the raw material auxiliary heating and vaporizing device (6) is used for heating and vaporizing the liquid hydrogen production raw material when the catalytic hydrogen production system is firstly cold started, and the catalytic hydrogen production system is closed after normal operation.
7. The catalytic hydrogen production system according to any one of claims 1 to 6, further comprising a gas-liquid separator (34), a hydrogen gas condenser (29) and a hydrogen gas purification processor (24) which are connected in sequence, wherein the gas-liquid separator (34) is communicated with the high-temperature hydrogen gas in the raw material vaporization superheater (7); the bottom of the raw material vaporization superheater (7) is connected with the bottom of the gas-liquid separator (34) through a condensate discharge valve (36), the bottom of the gas-liquid separator (34) is provided with a raw material liquid discharge port (35), and the raw material liquid discharge port (35) is used for discharging unreacted liquid hydrogen production raw materials.
8. A system for reducing nitrogen oxides by burning hydrogen, comprising a combustion device, a hydrogen burner and a catalytic hydrogen production system according to any one of claims 1 to 7, wherein the combustion device comprises a main combustion chamber (33) and a discharge flue arranged at the upper part of the main combustion chamber (33); the catalytic hydrogen production system sprays ignited hydrogen to the upper part of the combustion chamber (33) and/or the discharge flue through the hydrogen combustor, and the combusted hydrogen reduces nitrogen oxides contained in the flue gas at the upper part of the combustion chamber (33) and/or the discharge flue.
9. The system for reducing nitrogen oxide through hydrogen combustion as claimed in claim 8, wherein the hydrogen combustor comprises an outer sleeve (43), an ignition assembly, a central gas inlet pipeline (38), a hydrogen inlet pipeline, a hydrogen injection burner tip, a combustion head (47) and a flame-stabilizing combustion disc (49), wherein the side wall of the outer sleeve (43) is of a hollow structure, and a cooling medium is filled in the side wall; a central gas inlet pipeline (38) and a plurality of hydrogen gas inlet pipelines surrounding the periphery of the central gas inlet pipeline (38) are arranged in the outer sleeve (43); the flame stabilizing combustion disc (49) is arranged at the end part of the outer sleeve (43), and a combustion head (47), a plurality of hydrogen injection combustion nozzles distributed around the combustion head (47) and a plurality of cyclone ventilation holes are arranged on the flame stabilizing combustion disc (49); the combustion head (47) is connected with the central gas inlet pipeline (38) and is used for igniting hydrogen; each hydrogen injection burner is respectively connected with each hydrogen inlet pipeline;
the ignition assembly is arranged on one side of the combustion head (47) and used for igniting gas sprayed out of the combustion head (47).
10. The system for reducing nitrogen oxide through hydrogen combustion as claimed in claim 9, wherein a plurality of swirl guide grooves (50) are formed on the outer circumference of the flame holding combustion disc (49), and at least one set of swirl vent holes are formed on the end surface of the flame holding combustion disc (49) and are uniformly distributed along the circumferential direction; the cyclone ventilation holes are obliquely arranged, and wind led out from the cyclone ventilation holes and the cyclone guide grooves (50) rises spirally and is fully mixed with nitrogen oxides in hydrogen and flue gas.
11. The system for reducing nitrogen oxides by combusting hydrogen as claimed in claim 8, wherein the side wall of the discharge flue is of a water-cooled wall structure, and a water-cooled pipe is arranged in the discharge flue.
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