CN115947305A - Catalytic reforming hydrogen production reaction system for inerting fuel tank by tail gas - Google Patents
Catalytic reforming hydrogen production reaction system for inerting fuel tank by tail gas Download PDFInfo
- Publication number
- CN115947305A CN115947305A CN202211611980.XA CN202211611980A CN115947305A CN 115947305 A CN115947305 A CN 115947305A CN 202211611980 A CN202211611980 A CN 202211611980A CN 115947305 A CN115947305 A CN 115947305A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- fuel tank
- fuel
- inerting
- catalytic reforming
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000001257 hydrogen Substances 0.000 title claims abstract description 103
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 103
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 239000007789 gas Substances 0.000 title claims abstract description 71
- 239000002828 fuel tank Substances 0.000 title claims abstract description 54
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 52
- 238000001833 catalytic reforming Methods 0.000 title claims abstract description 45
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 28
- 239000000446 fuel Substances 0.000 claims abstract description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 230000003197 catalytic effect Effects 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 27
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000000295 fuel oil Substances 0.000 claims abstract description 13
- 150000001335 aliphatic alkanes Chemical class 0.000 claims abstract description 11
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 7
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical group [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 58
- 230000001105 regulatory effect Effects 0.000 claims description 40
- 239000012528 membrane Substances 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 31
- 229910052759 nickel Inorganic materials 0.000 claims description 30
- 239000012510 hollow fiber Substances 0.000 claims description 28
- 238000002156 mixing Methods 0.000 claims description 26
- 239000003054 catalyst Substances 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- 238000002309 gasification Methods 0.000 claims description 3
- 239000003350 kerosene Substances 0.000 abstract description 22
- 239000007795 chemical reaction product Substances 0.000 abstract description 15
- 238000000034 method Methods 0.000 description 9
- 239000002994 raw material Substances 0.000 description 7
- 238000005485 electric heating Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000005070 sampling Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 238000006057 reforming reaction Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Images
Classifications
-
- 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
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Abstract
The invention belongs to the technical field of aircraft power, and discloses a catalytic reforming hydrogen production reaction system with tail gas used for fuel tank inerting, which comprises a fuel tank, a water tank, a catalytic reactor and a hydrogen separator, wherein fuel oil in the fuel tank and water in the water tank are pumped out, and then are fully mixed and heated, and then enter the catalytic reactor to generate mixed gas comprising hydrogen, carbon monoxide, carbon dioxide and trace micromolecular alkane, the mixed gas is separated by the hydrogen separator, hydrogen is separated out for use by a fuel cell, and other gases are separated out, cooled to a certain temperature, and then are supplied to the fuel tank and are in an inerting state. The invention supplies hydrogen for the fuel cell by the real-time catalytic reforming reaction of the aviation kerosene, avoids the technical problems of safety, economy and the like caused by directly storing the hydrogen on the plane, has higher system safety and economy, is used for inerting the fuel tank after the rest reaction products are subjected to heat exchange and liquid removal, and has high system utilization efficiency.
Description
Technical Field
The invention belongs to the technical field of aircraft power, and relates to a catalytic reforming hydrogen production system for an aircraft, in particular to a catalytic reforming hydrogen production reaction system for inerting a fuel tank by tail gas.
Background
The fuel cell is an energy conversion device which can directly convert the chemical energy of the gasified fuel into electric energy and heat energy, has the energy conversion efficiency far exceeding that of an internal combustion engine, and has wide application prospect. Among them, hydrogen is the best fuel for fuel cells, so these cells using hydrogen as fuel are also called hydrogen fuel cells, which are the most widely used fuel cells.
Because the safe and efficient storage of hydrogen on the airplane is a technical bottleneck, the existing modes of high-pressure gaseous hydrogen storage, low-temperature liquid hydrogen storage, solid hydrogen storage and the like have great problems in the aspects of safety, economy, energy density and the like, so that the application of the hydrogen fuel cell on the airplane is greatly limited. The aviation kerosene is used as hydrocarbon fuel widely applied to various airplanes, and if the hydrogen is directly prepared from the aviation kerosene through catalytic reforming reaction and is further purified and supplied to a fuel cell, the aviation kerosene is more efficient and convenient to store and transport, and has higher energy density and use safety.
At present, the catalytic reforming hydrogen production by taking micromolecular alkanes such as methane, ethanol and the like as fuels is a high-efficiency hydrogen production method, but the method is difficult to apply in the aviation field due to different reaction raw materials (aviation kerosene components are very complex, the distribution of carbon atoms is mainly C7-C15, and the reaction raw materials comprise aromatic compounds, macromolecular alkanes, various trace thioether and ethers and the like) and different reaction mechanisms. With the continuous and deep research on the catalytic reforming hydrogen production of aviation kerosene in recent years, the scheme of producing hydrogen in real time through the catalytic reforming reaction of aviation kerosene and supplying the hydrogen to a fuel cell for power generation has certain feasibility, and on the basis of further solving the problems that the dynamic regulation energy of the system is poor (the current catalytic reforming reaction process is mostly a fixed working condition, and the catalytic reforming reaction working condition is complicated and changeable due to the change of the flying height and the great change of temperature and pressure in the airborne environment), and the energy conversion rate is low when the catalytic reforming reaction product hydrogen is low in purity, the catalytic reforming hydrogen production reaction system with the tail gas used for inerting the fuel tank is provided.
CN201710001549.6 proposes a system and a working method for inerting an aircraft fuel tank by catalytic reforming, wherein mixed gas (containing fuel steam, oxygen, nitrogen, carbon dioxide and the like) in the fuel tank is extracted, and after drying, pressurizing and separating, the fuel steam and the oxygen are catalytically reformed into carbon dioxide and hydrogen in a reforming reactor, and the catalytic reforming process generated in the reactor is actually an oxidation process and is not a catalytic reforming process; and the technical solution thereof cannot be realized because oxygen, which is one of the reaction raw materials of the technical solution thereof, oxidizes the generated hydrogen into water vapor in the reforming reactor thereof, and thus hydrogen cannot be generated at the rear end.
Disclosure of Invention
In order to solve the problems, the invention provides a catalytic reforming hydrogen production reaction system for inerting a fuel tank by tail gas, wherein aviation kerosene and steam are subjected to catalytic reforming reaction to produce hydrogen, hydrogen in reaction products is purified by a nickel-based hollow fiber membrane and then is supplied to a fuel cell, and the rest reaction products can be used for inerting the fuel tank after heat exchange treatment.
In order to realize the task, the invention adopts the following technical scheme:
a catalytic reforming hydrogen production reaction system with tail gas used for fuel tank inerting comprises a fuel tank, a water tank, a catalytic reactor and a hydrogen separator, wherein fuel oil in the fuel tank and water in the water tank are pumped out and then fully mixed and heated to enter the catalytic reactor to generate mixed gas comprising hydrogen, carbon monoxide, carbon dioxide and trace micromolecular alkane, the mixed gas is separated through the hydrogen separator, the hydrogen is separated out for use by a fuel cell, and other gases are separated out and then cooled to a certain temperature and then are supplied to the fuel tank and are in an inerting state.
The high-pressure fuel pump, the first flow regulating valve, the first check valve, the high-pressure water pump, the second flow regulating valve and the second check valve are further included, and the fuel in the fuel tank is mixed with water after being pressurized and regulated by the high-pressure fuel pump, the first flow regulating valve and the first check valve in sequence; the water in the water tank is mixed with the fuel oil after being pressurized and regulated by the high-pressure water pump, the second flow regulating valve and the second one-way valve in sequence.
And the rear ends of the first one-way valve and the second one-way valve are connected with the mixing preheating furnace, and the mixing preheating furnace is provided with a first heating device for heating the mixed liquid to a gasification state.
Furthermore, the catalytic reactor is provided with a second heating device, and the mixed gas is continuously heated to 750-800 ℃ in the catalytic reactor and undergoes catalytic reforming reaction. The conversion rate of the reaction raw materials and the selectivity of hydrogen in the temperature range can reach a better state.
Further, the inner surface of the catalytic reactor is coated with a catalyst of alumina modified by Pt and Ni.
Further, the hydrogen separator is specifically a nickel-based hollow fiber membrane module, and the nickel-based hollow fiber membrane module is provided with a mixed gas inlet, a hydrogen outlet and a mixed gas outlet.
Furthermore, the rear end of a hydrogen outlet of the hydrogen separator is connected with the fuel cell through a third flow regulator, and the back pressure at the front end of the hydrogen separator and the hydrogen flow entering the fuel cell are regulated through the third flow regulator.
Furthermore, the rear end of a mixed gas outlet of the hydrogen separator is connected with a fuel tank through a heat exchanger and a high-temperature cut-off valve, and the heat exchanger adopts ram air as a heat exchange device of the cold end heat sink or adopts fuel oil as a heat exchange device of the cold end heat sink.
Further, a gas-liquid separator is arranged between the heat exchanger and the high-temperature cut-off valve, the gas-liquid separator separates out condensed and separated liquid and then discharges the separated liquid, and gas is continuously conveyed to the rear end.
Compared with the prior art, the invention has the following technical characteristics:
1. the aviation kerosene is used for catalyzing and reforming reaction in real time to supply hydrogen for the fuel cell, so that the technical problems in the aspects of safety, economy, energy density and the like caused by directly storing hydrogen on an airplane are avoided, and the system has higher safety and economy;
2. compared with the existing catalytic reforming hydrogen production device, the system takes the application requirement of the airborne environment as a starting point, takes the aviation kerosene as a raw material, and the reaction product is separated and purified by the nickel-based hollow fiber membrane component, so that the energy efficiency of the fuel cell is further improved, and the rest reaction products can be used for inerting the fuel tank after heat exchange and liquid removal, and the energy utilization efficiency of the system is higher;
3. the system controls the raw material proportion of the aviation kerosene and the water vapor through the flow regulating valve, controls the reaction temperature in the reactor through the heating power of the reaction heating furnace, realizes the selectivity of the catalytic reforming reaction, can regulate the hydrogen flow supplied to the fuel cell by the system in real time, and has the advantages of strong selectivity of the catalytic reforming reaction product and strong dynamic regulation capability of the system.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some examples of the present invention, and therefore should not be considered as limiting the scope, and that for those skilled in the art, other related drawings can be obtained according to the drawings without inventive effort.
FIG. 1 is a schematic diagram of a catalytic reforming hydrogen production reaction system in which tail gas is used for fuel tank inerting according to the present invention;
FIG. 2 is a schematic diagram of a catalytic reforming hydrogen production reaction system using fuel oil as a cold end heat sink according to the present invention;
FIG. 3 is a graph of catalytic reforming reaction versus reaction temperature for the present invention;
the system comprises a fuel tank 1, a high-pressure fuel pump 2, a first flow regulating valve 3, a first one-way valve 4, a water tank 5, a high-pressure water pump 6, a second flow regulating valve 7, a second one-way valve 8, a mixed preheating furnace 9, a first heating device 10, a first temperature sensor 11, a first pressure sensor 12, a catalytic reactor 13, a second heating device 14, a second temperature sensor 15, a nickel-based hollow fiber membrane module 16, a third flow regulating valve 17, a fuel cell 18, a heat exchanger 19, a gas-liquid separator 20, a third temperature sensor 21, a high-temperature cut-off valve 22 and a controller 23.
Detailed Description
This section is an example of the present invention and is provided to explain and illustrate the technical solutions of the present invention. The embodiments of the invention and the features of the embodiments can be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate directions or positional relationships to give the drawings the orientation or positional relationships, and are used for convenience of description and simplicity of description, but do not indicate or imply that the device or case being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, 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 relative importance or implying any number of technical features indicated. Thus, features defined as "first", "second", etc. may explicitly or implicitly include more than one of the features. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it should be noted that unless otherwise explicitly stated or limited, the terms "mounted," "connected" and "connected" should be interpreted broadly, and may be, for example, a fixed connection, a detachable connection or an integrated connection; the connection can be mechanical connection or point connection; either directly or indirectly through intervening profiles, or both. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
A catalytic reforming hydrogen production reaction system with tail gas used for fuel tank inerting comprises a fuel tank 1, a water tank 5, a catalytic reactor 13 and a hydrogen separator, wherein fuel oil in the fuel tank 1 and water in the water tank 5 are pumped out, and then are fully mixed and heated, and then enter the catalytic reactor 13 to generate mixed gas containing hydrogen, carbon monoxide, carbon dioxide and trace small molecular alkane, the mixed gas is separated through the hydrogen separator, the hydrogen is separated out for a fuel cell 18, and other gases are separated out and then cooled to a certain temperature, are provided for the fuel tank 1 and are in an inerting state.
The high-pressure fuel pump 2, the first flow regulating valve 3, the first check valve 4, the high-pressure water pump 6, the second flow regulating valve 7 and the second check valve 8 are further included, and the fuel in the fuel tank 1 is mixed with water after being pressurized and regulated by the high-pressure fuel pump 2, the first flow regulating valve 3 and the first check valve 4 in sequence; the water in the water tank 5 is mixed with the fuel oil after being pressurized and regulated by the high-pressure water pump 6, the second flow regulating valve 7 and the second one-way valve 8 in sequence.
The device further comprises a mixing preheating furnace 9, the rear ends of the first one-way valve 4 and the second one-way valve 8 are connected with the mixing preheating furnace 9, and the mixing preheating furnace 9 is provided with a first heating device 10 for heating the mixed liquid to a gasification state.
The catalytic reactor 13 is provided with a second heating device 14, and the mixed gas is continuously heated to 750-800 ℃ in the catalytic reactor 13 and undergoes catalytic reforming reaction. The conversion rate of the reaction raw materials and the selectivity of hydrogen in the temperature range can reach a better state.
The inner surface of the catalytic reactor 13 is coated with a catalyst of alumina modified with Pt, ni.
The hydrogen separator is specifically a nickel-based hollow fiber membrane module 16, and the nickel-based hollow fiber membrane module 16 is provided with a mixed gas inlet, a hydrogen outlet and a mixed gas outlet.
The back end of the hydrogen outlet of the hydrogen separator is connected with the fuel cell 18 through a third flow regulator 17, and the back pressure at the front end of the hydrogen separator and the hydrogen flow entering the fuel cell 18 are regulated through the third flow regulator 17.
The rear end of a mixed gas outlet of the hydrogen separator is connected with the fuel tank 1 through a heat exchanger 19 and a high-temperature cut-off valve 22, and the heat exchanger 19 is a heat exchange device with ram air as a cold-end heat sink or a heat exchange device with fuel oil as a cold-end heat sink.
A gas-liquid separator 20 is further provided between the heat exchanger 19 and the high-temperature shut-off valve 22, and the gas-liquid separator 20 separates the condensed and precipitated liquid, discharges the separated liquid, and continuously sends the gas to the rear end.
The system also comprises a controller 23, wherein the controller 23 is connected with and controls all flow regulating valves, one-way valves, temperature and pressure sensors and heating devices in the system.
The following is another embodiment of the present invention.
The invention provides a catalytic reforming hydrogen production reaction system with tail gas used for fuel tank inerting, which generates a catalytic reforming hydrogen production reaction through aviation kerosene and steam, wherein hydrogen in reaction products is purified by a nickel-based hollow fiber membrane and supplied to a fuel cell, and the residual reaction products can be used for fuel tank inerting after heat exchange treatment.
As shown in fig. 1, the catalytic reforming hydrogen production reaction system for inerting a fuel tank with exhaust gas of the present invention comprises a fuel tank 1, a high-pressure fuel pump 2, a first flow regulating valve 3, a first check valve 4, a water tank 5, a high-pressure water pump 6, a second flow regulating valve 7, a second check valve 8, a mixing preheater 9, a first heating device 10, a first temperature sensor 11, a first pressure sensor 12, a catalytic reactor 13, a second heating device 14, a second temperature sensor 15, a nickel-based hollow fiber membrane module 16, a third flow regulating valve 17, a fuel cell 18, a heat exchanger 19, a gas-liquid separator 20, a third temperature sensor 21, a high-temperature cut-off valve 22, and a controller 23, wherein: the mixing preheating furnace 9 is provided with an aviation kerosene inlet, a water inlet, a mixed gas outlet, an electric heating anode and an electric heating cathode; the catalytic reactor 13 is provided with a preheating gas inlet, a reaction gas outlet, an electric heating anode and an electric heating cathode; the nickel-based hollow fiber membrane component 16 is provided with a mixed gas inlet, a hydrogen outlet and a mixed gas outlet;
an outlet of the fuel tank 1 is sequentially connected with a high-pressure fuel pump 2, a first flow regulating valve 3, a first one-way valve 4 and an aviation kerosene inlet of a mixing preheating furnace 9 through pipelines; an outlet of the water tank 5 is sequentially connected with a high-pressure water pump 6, a second flow regulating valve 7, a second one-way valve 8 and a water inlet of a mixing preheating furnace 9 through pipelines; a mixed gas outlet of the mixed preheating furnace 9 is connected with a preheated gas inlet of the catalytic reactor 13 through a pipeline, and a reaction gas outlet of the catalytic reactor 13 is connected with a mixed gas inlet of the nickel-based hollow fiber membrane module 16 through a pipeline; the electric heating anode of the mixing preheating furnace 9 is connected with the cathode of the first heating device 10 through an electric wire, and the electric heating cathode of the mixing preheating furnace 9 is connected with the anode of the first heating device 10 through an electric wire; the electrically heated anode of the catalytic reactor 13 is connected with the cathode of the second heating device 14 through a wire, and the electrically heated cathode of the catalytic reactor 13 is connected with the anode of the second heating device 14 through a wire; wherein, the catalytic reactor 13 is an integral catalytic reactor, the inner surface of which is coated with a catalyst of Pt and Ni modified alumina, which can catalytically reform aviation kerosene and water in a certain proportion into hydrogen, carbon dioxide, carbon monoxide and trace small molecular alkane at a certain temperature, and the proportion of the reaction product is selectable; the heating power of the first heating device 10 is adjustable so as to control the temperature of the gas at the outlet of the mixing preheating furnace 9; the heating power of the second heating device 14 is adjustable to adjust the reaction temperature in the catalytic reactor 13;
the first temperature sensor 11 is connected with a sampling port on a pipeline between the mixing preheating furnace 9 and the catalytic reactor 13; the first pressure sensor 12 is connected with a sampling port on a pipeline between the mixing preheating furnace 9 and the catalytic reactor 13; the second temperature sensor 15 is connected with a sampling port on a pipeline between the catalytic reactor 13 and the nickel-based hollow fiber membrane module 16; the first temperature sensor 11 is a K-type thermocouple temperature sensor, monitors the temperature of the mixed gas at the outlet of the mixing and preheating furnace 9, and provides a temperature signal for adjusting the heating power of the first heater 10; the first pressure sensor 12 monitors the pressure of the mixed gas at the outlet of the mixing preheating furnace 9 and provides signals for adjusting the pressurization values of the high-pressure fuel pump 2 and the high-pressure water pump 6;
a hydrogen outlet of the nickel-based hollow fiber membrane module 16 is sequentially connected with a third flow regulating valve 17 and a fuel cell 18 through pipelines; the nickel-based hollow fiber membrane component 16 is a membrane component with the interior composed of hundreds of fine membrane filaments, the membrane filaments only have permeation selectivity to hydrogen, the ideal separation rate is achieved within the temperature range of 600-900 ℃, the hydrogen in the high-temperature reaction product at the outlet of the catalytic reactor 13 can be extracted, the purity reaches more than 99%, compared with palladium-based hollow fiber membranes, the cost is high, the membrane preparation process is complex, the nickel-based hollow fiber membrane is cheap, the nickel-based hollow fiber membrane can be prepared into a self-supporting membrane to strengthen the structural stability of the membrane, and the nickel-based hollow fiber membrane component has good thermodynamic and chemical stability; the third flow regulating valve 17 is continuously adjustable, and the opening degree of the third flow regulating valve 17 is adjusted in time according to the flow requirement of the inlet of the fuel cell 18 and the backpressure requirement of the separation and purification of the nickel-based hollow fiber membrane module 16, so that the system works in a proper working condition mode; the fuel cell 18 specifically refers to a solid oxide fuel cell, which receives high-temperature and high-purity hydrogen purified by the nickel-based hollow fiber membrane module 16, is used for generating electricity by the fuel cell, and has the advantage of high energy conversion rate;
a mixed gas outlet of the nickel-based hollow fiber membrane module 16 is sequentially connected with a heat exchanger 19, a gas-liquid separator 20, a high-temperature cut-off valve 22 and an inlet of the fuel tank 1 through pipelines; the third temperature sensor 21 is connected with a sampling port on a pipeline between the gas-liquid separator 20 and the high-temperature cut-off valve 22; the heat exchanger 19 adopts a plate-fin heat exchanger, and heat sink at the cold end of the heat exchanger is ram air; the third temperature sensor 21 is used for monitoring the gas temperature at the outlet of the gas-liquid separator 20 and providing an input signal for the safe disconnection of the high-temperature cut-off valve 22 when the outlet temperature of the gas-liquid separator 20 is higher than a set value due to the failure or fault of the heat exchanger 19;
the controller 23 comprises a signal input end and a signal output end; the signal input end of the controller 23 is connected with the signal output ends of the first temperature sensor 11, the first pressure sensor 12, the second temperature sensor 15 and the third temperature sensor 21 in sequence through cables; the signal output end of the controller 23 is connected with the signal control ends of the high-pressure fuel pump 2, the first flow regulating valve 3, the high-pressure water pump 6, the second flow regulating valve 7, the first heating device 10, the second heating device 14, the third flow regulating valve 17 and the high-temperature cut-off valve 22 in sequence through cables.
Specifically, the working process of the catalytic reforming hydrogen production reaction system for inerting the fuel tank by using the tail gas is as follows:
preheating: the controller 23 sends a working signal (defined as an opening signal) to the high-pressure fuel pump 2 to extract the aviation kerosene in the fuel tank 1 and pressurize the aviation kerosene to a first working pressure, and meanwhile, the controller 23 sends a control signal to the first flow regulating valve 3 to regulate the aviation kerosene at the outlet of the high-pressure fuel pump 2 to a first working flow, and the aviation kerosene passes through the first check valve 4 and then is sent into the mixing preheating furnace 9; the controller 23 sends a working signal (defined as an opening signal) to the high-pressure water pump 6 to extract liquid water in the water tank 5 and pressurize the liquid water to a first working pressure, and simultaneously the controller 23 sends a control signal to the second flow regulating valve 7 to regulate water at the outlet of the high-pressure water pump 6 to a second working flow, and the water passes through the first one-way valve 8 and then is sent into the mixing preheating furnace 9; the controller 23 receives the gas pressure at the outlet of the mixing preheating furnace 9 monitored by the first pressure sensor 12, sends adjusting signals to the high-pressure fuel pump 2 and the high-pressure water pump 6 to keep the second working pressure in the mixing preheating furnace 9 stable, the controller 23 receives the gas temperature at the outlet of the mixing preheating furnace 9 monitored by the first temperature sensor 11, sends control signals to the first heating device 10 to adjust the heating power to keep the stable preheating temperature in the mixing preheating furnace 9, and the liquid aviation kerosene and the liquid water entering the mixing preheating furnace 9 absorb heat and are converted into aviation kerosene steam and water vapor which are fully mixed to reach the preheating temperature;
and (3) catalytic reforming process: the mixed gas reaching the preheating temperature enters the catalytic reactor 13, the controller 23 receives the gas temperature at the outlet of the catalytic reactor 13 monitored by the second temperature sensor 15, sends a control signal to the second heating device 14 to adjust the heating power so as to keep the stable reaction temperature in the catalytic reactor 13, and under the catalysis of a catalyst at high temperature, the aviation kerosene and steam undergo a reforming reaction to generate reaction products which mainly contain hydrogen and contain carbon dioxide, carbon monoxide and trace small molecular alkanes (such as CH4, C2H6, C2H4, C3H8 and the like), and because the catalytic reforming reaction has selectivity, the proportion of hydrogen content is increased in a proper temperature range, and the content of the small molecular alkanes is further reduced and can be lower than 0.1%;
hydrogen purification supply process: the high-temperature mixed gas at the outlet of the catalytic reactor 13 enters the nickel-based hollow fiber membrane module 16, the nickel-based membrane filaments in the nickel-based hollow fiber membrane module only have permeation selectivity to hydrogen and have an ideal separation rate in a certain high-temperature range, and the controller 23 sends a control signal to the third flow regulating valve 17 to regulate the back pressure of the hydrogen outlet of the nickel-based hollow fiber membrane module 16, so that the nickel-based hollow fiber membrane module 16 achieves the optimal separation efficiency, and the separated high-purity hydrogen is sent to a fuel cell;
and (3) tail gas treatment and utilization process: the residual reaction products at the mixed gas outlet of the nickel-based hollow fiber membrane component 16 mainly comprise carbon dioxide, carbon monoxide, trace hydrogen and trace micromolecular alkane (such as CH4, C2H6, C2H4, C3H8 and the like), the residual reaction products enter the heat exchanger 19, the temperature is reduced to the ambient temperature after the residual reaction products fully exchange heat with the ram air at the cold end, condensed liquid alkane is separated out through the gas-liquid separator 20, when the outlet gas temperature of the gas-liquid separator 20 monitored by the third temperature sensor 21 received by the controller 23 is lower than the high-temperature protection temperature, the high-temperature cut-off valve 22 is kept in an open state, the residual gas is sent into the fuel tank 1 through the high-temperature cut-off valve 22, the oxygen concentration of the gas phase space in the fuel tank 1 is reduced, and accordingly inerting of the fuel tank is realized; when the gas-liquid separator 20 outlet gas temperature monitored by the third temperature sensor 21 received by the controller 23 is higher than or equal to the set high-temperature protection temperature, the controller 23 sends a cut-off signal to the high-temperature cut-off valve 22 to prevent the high-temperature gas from entering the fuel tank, which brings danger.
Example 2:
in this embodiment, fuel oil is used as a cold end heat sink of the heat exchanger 19, and as shown in fig. 2, the difference between this system and embodiment 1 is that the cold end heat exchange medium of the heat exchanger 19 is fuel oil.
Claims (9)
1. The catalytic reforming hydrogen production reaction system is characterized by comprising a fuel tank (1), a water tank (5), a catalytic reactor (13) and a hydrogen separator, wherein fuel oil in the fuel tank (1) and water in the water tank (5) are pumped out, and then are fully mixed and heated to enter the catalytic reactor (13) to generate mixed gas comprising hydrogen, carbon monoxide, carbon dioxide and trace micromolecular alkane, the mixed gas is separated by the hydrogen separator, the hydrogen is separated to be used for a fuel cell (18), and other gases are cooled to a certain temperature after being separated to be supplied to the fuel tank (1) and enable the fuel tank to be in an inerting state.
2. The catalytic reforming hydrogen production reaction system for inerting the fuel tank by tail gas as claimed in claim 1, further comprising a high-pressure fuel pump (2), a first flow regulating valve (3), a first check valve (4), a high-pressure water pump (6), a second flow regulating valve (7) and a second check valve (8), wherein the fuel in the fuel tank (1) is mixed with water after being pressurized and regulated by the high-pressure fuel pump (2), the first flow regulating valve (3) and the first check valve (4) in sequence; water in the water tank (5) is mixed with fuel oil after being pressurized and regulated by the high-pressure water pump (6), the second flow regulating valve (7) and the second one-way valve (8) in sequence.
3. The catalytic reforming hydrogen production reaction system for inerting the fuel tank by tail gas as claimed in claim 2, further comprising a mixing preheating furnace (9), wherein the rear ends of the first check valve (4) and the second check valve (8) are connected with the mixing preheating furnace (9), and the mixing preheating furnace (9) is provided with a first heating device (10) for heating the mixed liquid to a gasification state.
4. The catalytic reforming hydrogen production reaction system for inerting a fuel tank by tail gas as set forth in claim 1, wherein the catalytic reactor (13) is provided with a second heating device (14), and the mixed gas is continuously heated to 750 ℃ to 800 ℃ in the catalytic reactor (13) and the catalytic reforming reaction is carried out.
5. The catalytic reforming hydrogen production reaction system using tail gas for fuel tank inerting as claimed in claim 1, wherein the inner surface of the catalytic reactor (13) is coated with a catalyst of alumina modified with Pt, ni.
6. The catalytic reforming hydrogen production reaction system for inerting the fuel tank by tail gas as claimed in claim 1, wherein the hydrogen separator is a nickel-based hollow fiber membrane module (16), and the nickel-based hollow fiber membrane module (16) is provided with a mixed gas inlet, a hydrogen outlet and a mixed gas outlet.
7. The catalytic reforming hydrogen production reaction system for inerting the fuel tank by tail gas as claimed in claim 6, wherein the back end of the hydrogen outlet of the hydrogen separator is connected with the fuel cell (18) through a third flow regulator (17), and the back pressure at the front end of the hydrogen separator and the hydrogen flow entering the fuel cell (18) are regulated through the third flow regulator (17).
8. The catalytic reforming hydrogen production reaction system for inerting the fuel tank by tail gas as claimed in claim 7, wherein the rear end of the mixed gas outlet of the hydrogen separator is connected with the fuel tank (1) through a heat exchanger (19) and a high-temperature shut-off valve (22), and the heat exchanger (19) is a heat exchange device using ram air as a cold-end heat sink or a heat exchange device using fuel oil as a cold-end heat sink.
9. The catalytic reforming hydrogen production reaction system for inerting the fuel tank as defined in claim 8, wherein a gas-liquid separator (20) is further provided between the heat exchanger (19) and the high temperature shut-off valve (22), the gas-liquid separator (20) separates out condensed and separated liquid and discharges the separated liquid, and the gas is continuously sent to the rear end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211611980.XA CN115947305A (en) | 2022-12-14 | 2022-12-14 | Catalytic reforming hydrogen production reaction system for inerting fuel tank by tail gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211611980.XA CN115947305A (en) | 2022-12-14 | 2022-12-14 | Catalytic reforming hydrogen production reaction system for inerting fuel tank by tail gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115947305A true CN115947305A (en) | 2023-04-11 |
Family
ID=87297516
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211611980.XA Pending CN115947305A (en) | 2022-12-14 | 2022-12-14 | Catalytic reforming hydrogen production reaction system for inerting fuel tank by tail gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115947305A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117347548A (en) * | 2023-12-04 | 2024-01-05 | 中国航空工业集团公司金城南京机电液压工程研究中心 | Fuel oil regeneration cooling test system and control method |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106741984A (en) * | 2017-01-03 | 2017-05-31 | 南京航空航天大学 | A kind of system and its method of work of catalytic reforming inerting aircraft fuel tank |
| CN107867404A (en) * | 2017-11-20 | 2018-04-03 | 南京航空航天大学 | The apparatus and method of fuel tank inerting |
| CN107890783A (en) * | 2017-12-15 | 2018-04-10 | 天津工业大学 | A kind of metallic nickel hollow fiber film assembly and preparation method thereof and the method using its separation hydrogen |
| CN110165260A (en) * | 2019-05-28 | 2019-08-23 | 北京中科三鼎科技有限公司 | A kind of efficient silent formula power generator reformed based on fuel catalytic |
| US20200078726A1 (en) * | 2018-09-11 | 2020-03-12 | Hamilton Sundstrand Corporation | Electrochemical drying of humid inert gas for fuel tank inerting |
| CN110890572A (en) * | 2019-11-06 | 2020-03-17 | 华中科技大学 | Solid oxide fuel cell power generation system based on oil fuel |
| CN114313279A (en) * | 2021-12-28 | 2022-04-12 | 中国航空工业集团公司金城南京机电液压工程研究中心 | Catalytic inerting system with bypass branch control and control method |
| CN114538374A (en) * | 2022-03-18 | 2022-05-27 | 中国科学院生态环境研究中心 | Device system for reforming and producing hydrogen by vehicle-mounted bioethanol and reforming and hydrogen production method |
-
2022
- 2022-12-14 CN CN202211611980.XA patent/CN115947305A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106741984A (en) * | 2017-01-03 | 2017-05-31 | 南京航空航天大学 | A kind of system and its method of work of catalytic reforming inerting aircraft fuel tank |
| CN107867404A (en) * | 2017-11-20 | 2018-04-03 | 南京航空航天大学 | The apparatus and method of fuel tank inerting |
| CN107890783A (en) * | 2017-12-15 | 2018-04-10 | 天津工业大学 | A kind of metallic nickel hollow fiber film assembly and preparation method thereof and the method using its separation hydrogen |
| US20200078726A1 (en) * | 2018-09-11 | 2020-03-12 | Hamilton Sundstrand Corporation | Electrochemical drying of humid inert gas for fuel tank inerting |
| CN110165260A (en) * | 2019-05-28 | 2019-08-23 | 北京中科三鼎科技有限公司 | A kind of efficient silent formula power generator reformed based on fuel catalytic |
| CN110890572A (en) * | 2019-11-06 | 2020-03-17 | 华中科技大学 | Solid oxide fuel cell power generation system based on oil fuel |
| CN114313279A (en) * | 2021-12-28 | 2022-04-12 | 中国航空工业集团公司金城南京机电液压工程研究中心 | Catalytic inerting system with bypass branch control and control method |
| CN114538374A (en) * | 2022-03-18 | 2022-05-27 | 中国科学院生态环境研究中心 | Device system for reforming and producing hydrogen by vehicle-mounted bioethanol and reforming and hydrogen production method |
Non-Patent Citations (1)
| Title |
|---|
| 斯派莎克工程（中国）有限公司: "《蒸汽和冷凝水系统手册》", 31 January 2007, 上海科学技术文献出版社, pages: 724 - 725 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117347548A (en) * | 2023-12-04 | 2024-01-05 | 中国航空工业集团公司金城南京机电液压工程研究中心 | Fuel oil regeneration cooling test system and control method |
| CN117347548B (en) * | 2023-12-04 | 2024-02-06 | 中国航空工业集团公司金城南京机电液压工程研究中心 | Fuel oil regeneration cooling test system and control method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101222975B (en) | Compact reforming reactor | |
| US20140356738A1 (en) | Ammonia based system to prepare and utilize hydrogen to produce electricity | |
| JP2024518985A (en) | Systems and methods for processing ammonia | |
| Lukyanov et al. | Catalytic reactors with hydrogen membrane separation | |
| CN115947305A (en) | Catalytic reforming hydrogen production reaction system for inerting fuel tank by tail gas | |
| KR102190939B1 (en) | Ship | |
| Binazadeh et al. | Membrane reactors for hydrogen generation: From single stage to integrated systems | |
| CN113292045A (en) | Methanol water reforming hydrogen production system and control method | |
| RU2638350C1 (en) | Integrated membrane-catalytic reactor and coproduction method of synthesis gas and ultrapure hydrogen | |
| KR102355411B1 (en) | Ship | |
| CN101295795A (en) | Alkane cracking and fuel cell compound power generation system | |
| KR102355412B1 (en) | Fuel cell system and ship having the same | |
| KR102190948B1 (en) | Ship | |
| CN111453697B (en) | Multi-fuel universal reforming hydrogen production system and method for SOFC | |
| CN111620304A (en) | Hydrogen preparation method | |
| KR102190938B1 (en) | Ship | |
| KR102106656B1 (en) | Ship | |
| KR102190941B1 (en) | Ship | |
| CN115285939B (en) | Bioethanol autothermal reforming hydrogen production system | |
| Horng et al. | Reforming performance of a plasma-catalyst hybrid converter using low carbon fuels | |
| CN218841707U (en) | Self-heating and self-pressurizing efficient ammonia decomposition hydrogen production system | |
| US20230116672A1 (en) | Solid oxide fuel cell systems and methods of operating solid oxide fuel cell systems | |
| Aghaeinejad-Meybodi et al. | Solar Energy for Pure Hydrogen Production Using Inorganic Membrane Reactor | |
| KR20170080945A (en) | Ship | |
| KR20170015822A (en) | Fuel cell system and ship having the same |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |