CN113332933B - On-vehicle organic liquid hydride dehydrogenation reactor - Google Patents
On-vehicle organic liquid hydride dehydrogenation reactor Download PDFInfo
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- CN113332933B CN113332933B CN202110609331.5A CN202110609331A CN113332933B CN 113332933 B CN113332933 B CN 113332933B CN 202110609331 A CN202110609331 A CN 202110609331A CN 113332933 B CN113332933 B CN 113332933B
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- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 111
- 239000007788 liquid Substances 0.000 title claims abstract description 86
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- 238000007084 catalytic combustion reaction Methods 0.000 claims abstract description 69
- 239000003054 catalyst Substances 0.000 claims abstract description 68
- 239000007789 gas Substances 0.000 claims abstract description 61
- 239000001257 hydrogen Substances 0.000 claims abstract description 57
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- 238000000926 separation method Methods 0.000 claims abstract description 25
- 238000009826 distribution Methods 0.000 claims abstract description 20
- 230000003647 oxidation Effects 0.000 claims abstract description 14
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 14
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- 239000001301 oxygen Substances 0.000 claims abstract description 3
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- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 description 3
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- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
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- 229910052799 carbon Inorganic materials 0.000 description 1
- ZMIGMASIKSOYAM-UHFFFAOYSA-N cerium Chemical compound [Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce][Ce] ZMIGMASIKSOYAM-UHFFFAOYSA-N 0.000 description 1
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- 230000005484 gravity Effects 0.000 description 1
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- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D209/00—Heterocyclic compounds containing five-membered rings, condensed with other rings, with one nitrogen atom as the only ring hetero atom
- C07D209/56—Ring systems containing three or more rings
- C07D209/80—[b, c]- or [b, d]-condensed
- C07D209/82—Carbazoles; Hydrogenated carbazoles
- C07D209/86—Carbazoles; Hydrogenated carbazoles with only hydrogen atoms, hydrocarbon or substituted hydrocarbon radicals, directly attached to carbon atoms of the ring system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/12—Radiant burners
- F23D14/18—Radiant burners using catalysis for flameless combustion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a vehicle-mounted organic liquid hydride dehydrogenation reactor, which comprises an upper dehydrogenation reaction zone and a lower catalytic combustion zone, wherein the dehydrogenation reaction zone and the catalytic combustion zone are isolated from each other; the catalytic combustion zone is filled with a catalytic oxidation catalyst for hydrogen catalytic combustion reaction; the left side of the catalytic combustion zone is provided with a mixed gas distribution zone, and the right side of the catalytic combustion zone is provided with a tail gas collection zone; the mixed gas distribution area is used for uniformly distributing the mixed gas of hydrogen and oxygen; a heat pipe is vertically arranged in the catalytic combustion zone; the heat pipe penetrates through the catalytic combustion zone and the dehydrogenation reaction zone; the dehydrogenation reaction zone is arranged at the upper part of the catalytic combustion zone, and is internally filled with a dehydrogenation catalyst; the upper part of the dehydrogenation reaction zone is provided with a gas-liquid separation zone; the height of the dehydrogenation reaction zone is 1.1-1.5 times of the height of the catalytic combustion zone. The reactor has compact structure, convenient disassembly, high heat transfer efficiency and safe use, and can realize self-heating to generate hydrogen.
Description
Technical Field
The invention belongs to the technical field of organic liquid hydride dehydrogenation, and particularly relates to a novel vehicle-mounted organic liquid hydride dehydrogenation reactor.
Background
With the exhaustion of energy sources and the increasing severe environment, people are searching for alternative green energy sources, wherein hydrogen energy is green and pollution-free and has wide sources, but the hydrogen energy also has problems in aspects of storage, transportation and the like. The organic liquid is a hydrogen storage carrier, is liquid at normal temperature and pressure and is similar to gasoline, and can be directly transported and stored by using the existing infrastructure. However, the organic liquid is changed into organic liquid hydride after being hydrogenated, heat is required to be supplied during dehydrogenation of the organic liquid hydride, and the dehydrogenation temperature of most of the organic liquid hydride is high, so that the dehydrogenation catalyst is deactivated due to the fact that the dehydrogenation temperature is too high, and the dehydrogenation effect is affected due to the fact that heat transfer is uniform and heat transfer efficiency is high.
There has been some progress in finding efficient dehydrogenation catalysts and lower dehydrogenation temperature organic liquid hydrides, but less research has been conducted on the heat and mass transfer of dehydrogenation reactions. At present, most of heating modes such as electric heating, microwave heating, direct combustion and the like are adopted for heating the organic liquid hydride dehydrogenation reaction, the heating modes have the problems of low energy utilization rate, more auxiliary equipment of a system and lower heat transfer efficiency, and in addition, after the organic liquid hydride dehydrogenation, a large amount of hydrogen can carry part of organic liquid, and gas-liquid separation is required to be carried out after a reactor, so that the problems are unfavorable for the practical application of the organic liquid hydride dehydrogenation technology.
The heat pipe is used for heat transfer by utilizing the phase change of the working medium, has very good heat conductivity and temperature uniformity, and can avoid the deactivation of the dehydrogenation catalyst caused by the local overheating of the reactor when being used in the dehydrogenation reactor, and can obtain very good heat transfer efficiency; the catalytic combustion technology can enable fuel to burn stably and completely, reduce the burning temperature and reduce the generation of harmful gas, the technology can just provide heat for dehydrogenation reaction without deactivation of a dehydrogenation catalyst caused by too high temperature, hydrogen can be subjected to catalytic combustion, so that a small part of hydrogen generated by the dehydrogenation reaction is used as a reactant of the catalytic combustion, and the hydrogen catalytic combustion reaction provides heat for the dehydrogenation reaction. Therefore, the hydrogen catalytic combustion reaction and the organic liquid hydride dehydrogenation reaction and even the gas-liquid separation process can be integrated into one reactor, so that the energy utilization rate of the whole system is improved, and the structure of the whole system is more compact.
Disclosure of Invention
The invention aims to solve the problems of low heat transfer efficiency, uneven heat transfer, huge volume, complex structure and more needed auxiliary equipment of an organic liquid hydride dehydrogenation reactor and provides a novel vehicle-mounted organic liquid hydride dehydrogenation reactor. The reactor has the advantages of uniform heat transfer, high heat transfer efficiency, compact and easy disassembly, self-heating dehydrogenation, gas-liquid internal separation and the like.
The invention solves the problems by adopting the following technical scheme:
an on-vehicle organic liquid hydride dehydrogenation reactor comprises an upper dehydrogenation reaction zone and a lower catalytic combustion zone, wherein the dehydrogenation reaction zone and the catalytic combustion zone are isolated from each other;
the catalytic combustion zone is filled with a catalytic oxidation catalyst for hydrogen catalytic combustion reaction; the left side of the catalytic combustion zone is provided with a mixed gas distribution zone, and the right side of the catalytic combustion zone is provided with a tail gas collection zone; the mixed gas distribution area is used for uniformly distributing the mixed gas of hydrogen and oxygen; a heat pipe is vertically arranged in the catalytic combustion zone; the heat pipe penetrates through the catalytic combustion zone and the dehydrogenation reaction zone;
the dehydrogenation reaction zone is arranged at the upper part of the catalytic combustion zone, and the dehydrogenation catalyst is filled in the dehydrogenation reaction zone; the upper part of the dehydrogenation reaction zone is provided with a gas-liquid separation zone;
the height of the dehydrogenation reaction zone is 1.1-1.5 times of the height of the catalytic combustion zone.
As a further improvement of the invention, the mixed gas distribution area is of a horn-shaped structure, the section of the mixed gas distribution area is in an isosceles trapezoid, and the base angle of the trapezoid is 60-90 DEG
As a further improvement of the invention, the mixed gas distribution area is filled with a porous medium with the porosity of 80-98% and the pore diameter of 0.1-1.5 mm, which has the functions of promoting the mixing of air and hydrogen, redistributing the mixed gas of hydrogen and air and preventing tempering.
As a further improvement of the invention, the catalytic oxidation catalyst filled in the catalytic combustion zone catalyzes the oxidation of hydrogen at 150-500 ℃.
As a further improvement of the invention, the catalytic oxidation catalyst consists of a catalyst matrix, a catalyst carrier and a catalyst active component;
the catalyst matrix is an integral porous medium, the porosity of the porous medium is 85-95%, and the aperture is 0.5-2 mm; the matrix can be porous structural materials such as foam metal, cordierite, a wire mesh and the like;
the catalyst carrier is metal oxide loaded on a catalyst matrix, and the loading capacity is 0.5-20wt%; the carrier is loaded on the matrix by methods such as an impregnation method, a coating method, an ion exchange method and the like, and the materials include, but are not limited to, materials such as aluminum oxide, magnesium oxide, titanium oxide and the like;
the active component of the catalyst is noble metal loaded on a catalyst carrier, and the loading amount is 0.1-2 wt%; the active components are loaded on the catalyst carrier by methods such as an impregnation method, a coating method, an ion exchange method and the like, and the active components comprise noble metals such as palladium, platinum, rhodium and the like;
in addition, the hydrogen low-temperature catalytic oxidation catalyst can be added with an auxiliary agent to increase the cohesive force among a matrix, a carrier and active components, reduce the use amount of noble metals, and the auxiliary agent can be oxides of elements such as cerium, zirconium and the like, and has the load amount of 1-10 wt%.
As a further improvement of the invention, the working medium in the heat pipe is water, and the pipe wall material is a metal material; the number of the heat pipes can be regulated according to the size of the reactor, the number is generally 4-50, and the arrangement modes can be regular triangle, corner triangle, regular square or corner regular square; the distance from the lower end of the heat pipe to the bottom of the reactor is more than or equal to 5mm, and the distance from the upper end of the heat pipe to the organic liquid outlet/organic liquid hydride inlet is more than or equal to 5mm.
As a further improvement of the invention, the cross section of the tail gas collecting area is in an isosceles trapezoid shape, and the bottom angle of the trapezoid is 60-90 degrees; and one end of the tail gas collecting area with smaller inner diameter is connected with a tail gas outlet.
As a further improvement of the invention, the dehydrogenation reaction zone is filled with an integral dehydrogenation catalyst, and the dehydrogenation catalyst is provided with a plurality of through holes for placing heat pipes;
the dehydrogenation catalyst consists of a catalyst matrix, a catalyst carrier and a catalyst active component;
the catalyst matrix comprises but is not limited to porous materials such as foam metal, cordierite, wire mesh and the like, the porosity of the porous medium is 85% -98%, and the pore diameter is 1-3 mm;
the catalyst carrier comprises, but is not limited to, alumina, silica, graphite, activated carbon and other materials, and the loading amount of the carrier is 1-20wt%;
the catalyst active components comprise materials such as platinum, palladium, rhodium, nickel, copper and the like, and the loading amount of the active components is 0.1-20wt%.
As a further improvement of the invention, the gas-liquid separation area is provided with a metal net with the thickness of 1 cm-10 cm; the bottom of the metal net is 1cm to 5cm away from the dehydrogenation reaction zone, so that the separation of hydrogen and organic liquid is facilitated; the metal net can adsorb and condense organic liquid to achieve the purpose of gas-liquid separation. A hydrogen outlet is arranged at the top of the gas-liquid separation zone.
As a further improvement of the present invention, the dehydrogenation reaction zone and the catalytic combustion zone are separated by a metal plate.
The catalytic combustion technology can be started at normal temperature, and the catalytic combustion temperature can be controlled at 150-500 ℃ by adjusting parameters such as the proportion of mixed gas, airspeed and the like; the dehydrogenation reaction temperature is 180-300 ℃.
The invention couples the hydrogen catalytic combustion reaction and the organic liquid hydride dehydrogenation reaction into one reactor, can realize the integration of heat and hydrogen production, and reduces the size of the reactor and the use of matched facilities; the hydrogen generated by the dehydrogenation reaction can be used for catalyzing the combustion reaction, and the heat generated by the hydrogen catalyzing combustion reaction can be used for supplying heat for the dehydrogenation reaction, so that the hydrogen and the heat are mutually coupled, and the energy use efficiency of the reactor is improved; the heat pipe has ultrahigh heat conductivity and uniform temperature, and the heat pipe is used for transmitting heat between catalytic combustion reaction and dehydrogenation reaction, so that deactivation of a dehydrogenation reaction catalyst caused by hot spots of the reactor can be avoided; the dehydrogenation reaction of the organic liquid hydride can release a large amount of hydrogen, and the integral catalyst is filled in the dehydrogenation reaction zone, so that the contact area between the reactant and the catalyst is increased, the heat conductivity and the temperature uniformity of the reactor are improved, and the reactor of the integral catalyst has lower pressure drop; the gas-liquid separation area is arranged in the reactor, so that the system is more compact and is convenient to apply in a mobile device.
Drawings
FIG. 1 is a schematic structural diagram of a novel in-vehicle organic liquid hydride dehydrogenation reactor according to example 1;
in fig. 1: 1-mixed gas inlet, 2-mixed gas distribution area, 3-catalytic combustion area, 4-heat pipe, 5-tail gas collection area, 6-tail gas outlet, 7-organic liquid outlet, 8-dehydrogenation reaction area, 9-organic liquid hydride inlet, 10-metal net, 11-gas-liquid separation area, 12-hydrogen outlet.
FIG. 2 is a schematic diagram of a heat pipe arrangement.
FIG. 3 is a schematic structural diagram of a novel on-board organic liquid hydride dehydrogenation reactor according to example 2;
in fig. 3: 1-mixed gas inlet, 2-mixed gas distribution area, 3-catalytic combustion area, 4-heat pipe, 5-tail gas collection area, 6-tail gas outlet, 7-organic liquid hydride inlet, 8-dehydrogenation reaction area, 9-organic liquid outlet, 10-metal net, 11-gas-liquid separation area, 12-hydrogen outlet.
Detailed Description
The technical solutions in the embodiments of the present invention will be described in detail below with reference to the accompanying drawings, but the embodiments of the present invention are not limited thereto.
Example 1
Fig. 1 is a schematic structural diagram of a novel vehicle-mounted organic liquid hydride dehydrogenation reactor, which comprises an upper dehydrogenation reaction zone 8 and a lower catalytic combustion zone 3, wherein a mixed gas inlet 1 and a mixed gas distribution zone 2 are sequentially arranged on the left side of the catalytic combustion zone 3, and a tail gas collecting zone 5 and a tail gas outlet 6 are sequentially arranged on the right side of the catalytic combustion zone. The upper part of the dehydrogenation reaction zone 8 is provided with a gas-liquid separation zone 11, the gas-liquid separation zone 11 comprises a metal net 10, and the top of the gas-liquid separation zone 11 is provided with a hydrogen outlet 12. The dehydrogenation reaction zone 8 is positioned right above the catalytic combustion zone 3, and is separated from each other by a metal plate, the metal plate is fixedly provided with a heat pipe 4, and the heat pipe 4 penetrates through the dehydrogenation reaction zone 8 and the catalytic combustion zone 3. The upper side wall of the left side of the dehydrogenation reaction zone 8 is provided with an organic liquid outlet 7, the lower side wall of the right side is provided with an organic liquid hydride inlet 9, a gas-liquid separation zone 11 is positioned above the dehydrogenation reaction zone 8, and a metal net 10 is arranged in the gas-liquid separation zone 11, so that gas cooling and liquid absorption can be accelerated.
The porous medium is arranged in the gas distribution area 2, so that the mixed gas is uniformly distributed, tempering can be prevented in the catalytic combustion process, and the potential safety hazard of explosion caused by tempering is avoided; the catalytic combustion zone 3 is filled with a hydrogen low-temperature catalytic oxidation catalyst, the dehydrogenation reaction zone 8 is filled with a dehydrogenation reaction catalyst, the two catalysts are composed of a matrix, a carrier and active components, the matrix is in a porous medium structure form of cordierite, foam metal, a wire mesh and the like, the carrier is uniformly attached to the matrix, the hydrogen low-temperature catalytic oxidation catalyst carrier is alumina, magnesia, titania and other metal oxides, and the dehydrogenation reaction catalyst carrier can be alumina, silica, graphite, active carbon and the like; the active components of the hydrogen low-temperature catalytic oxidation catalyst are uniformly distributed on the carrier, and the material can be noble metal catalysts such as platinum, palladium, rhodium and the like, and the active components of the dehydrogenation catalyst are uniformly distributed on the carrier, and the material can be noble metal catalysts such as platinum, palladium, rhodium and the like or non-noble metal catalysts such as nickel, copper and the like; the heat pipe 4 is a gravity heat pipe, the heat pipe 4 is made of metal, working medium in the pipe is water, etc., and the arrangement mode of the heat pipe 4 on the metal plate can be regular triangle, corner regular triangle, regular square, corner regular square as shown in figure 2.
The organic liquid is a mixture of one or more of unsaturated aromatic compounds and/or heterocyclic unsaturated compounds and a solvent; the organic liquid hydride is a product obtained by hydrogenating the corresponding organic liquid. The unsaturated aromatic compounds include, but are not limited to, benzene, toluene, naphthalene, paraxylene, derivatives thereof, and the like; the heterocyclic unsaturated compounds include, but are not limited to, carbazole, indole, N-methyl/ethyl/propyl carbazole, N-methyl/ethyl/propyl indole, furans, pyridines, quinolines, derivatives thereof, and the like; the solvent includes, but is not limited to, one or more of methanol, ethanol, ethylene glycol, ethyl formate, n-butyl ether, methylene chloride, cyclohexane, naphthalene, etc.
The reactor mainly comprises two processes of hydrogen catalytic combustion heat supply and organic liquid hydride dehydrogenation, wherein when the dehydrogenation reactor runs stably, the two reactions are carried out simultaneously, and heat transfer and heat absorption are mutually coupled.
The heating process of the hydrogen catalytic combustion reaction is specifically described as follows: firstly, hydrogen and air enter a gas distribution area 2 from a mixed gas inlet through mixing, a porous medium is filled in the gas distribution area 2, the mixed gas enters a catalytic combustion area 3 after being uniformly distributed, the mixed gas undergoes catalytic combustion reaction under the action of a catalyst to release a large amount of heat, and the released heat rapidly heats a heat pipe 4 through heat convection and heat conduction of the porous medium; the mixed gas after catalytic combustion enters a tail gas collecting area 5, gradually converges in the tail gas collecting area 5, and finally flows out of the reactor through a tail gas outlet 6.
The organic liquid hydride dehydrogenation reaction process is specifically described as follows: while hydrogen catalytic combustion reaction is carried out, organic liquid hydride enters the reactor from an organic liquid hydride inlet 9 and then enters a dehydrogenation reaction zone 8, heat emitted by a heat pipe 4 heated by the catalytic combustion reaction is conducted to a surrounding porous medium, the organic liquid hydride is rapidly heated to the dehydrogenation reaction temperature to release hydrogen when passing through, the hydrogen rapidly rises through pores of the porous medium and is discharged out of the dehydrogenation reaction zone 8 to enter a gas-liquid separation zone 11, the organic liquid is cooled by a metal net 10 in the gas-liquid separation zone 11 and gradually converged into drops to the dehydrogenation reaction zone 8, and the hydrogen finally leaves the reactor from a hydrogen outlet 12 at the top of the reactor through the gas-liquid separation zone 11; most of the dehydrogenated organic liquid and the organic liquid collected from the gas-liquid separation zone 11 flow out of the reactor through the organic liquid outlet 7.
Example 2
The difference between the novel on-vehicle organic liquid hydride dehydrogenation reactor and the embodiment 1 is that the mixed gas flow direction of the embodiment 1 and the organic liquid flow direction are countercurrent, and the mixed gas flow direction of the embodiment 2 and the organic liquid flow direction are cocurrent, that is, the organic liquid hydride inlet of the embodiment 2 is positioned on the upper left side wall of the dehydrogenation reaction zone, and the organic liquid outlet is positioned on the lower right side wall of the dehydrogenation reaction zone, as shown in fig. 3.
Example 3
This example illustrates the dehydrogenation of perhydro N-ethylcarbazole.
The perhydro N-ethylcarbazole is subjected to dehydrogenation reaction in a dehydrogenation reaction zone to finally generate N-ethylcarbazole and hydrogen, and the chemical equation is as follows:
C 14 H 25 N→C 14 H 13 N+6H 2
most of hydrogen generated by the dehydrogenation reaction is used for generating electricity by a fuel cell, and the other part of hydrogen is subjected to catalytic combustion reaction in a catalytic combustion zone to provide heat for the dehydrogenation reaction. The hydrogen catalytic combustion reaction is as follows:
H 2 +1/2O 2 →H 2 O
the reactor of the embodiment is a dehydrogenation reactor with a unit volume of 2.5L for the dehydrogenation reaction of organic liquid hydride and the catalytic combustion reaction coupled with self-heating hydrogen production, and the produced hydrogen can meet the normal use of a 1kw fuel cell. The main body of the reactor is 200mm multiplied by 100mm, the height of the catalytic combustion zone is 40mm, and the height of the dehydrogenation reaction zone is 45mm. The dehydrogenation reaction zone is filled with foam nickel with the porosity of 90% and the pore size of 2mm as a catalyst matrix, the loading of the carrier alumina is 5wt% and the loading of the active component palladium is 0.5wt%; the catalytic combustion reaction zone is filled with foam nickel with the porosity of 95 percent as a catalyst matrix, the loading of the carrier alumina is 10 weight percent, and the loading of the active component platinum is 1 weight percent; the mixed gas distribution area was filled with a porous medium having a porosity of 98% and a pore size of 0.5 mm.
When the reactor normally operates, the perhydro N-ethylcarbazole enters the dehydrogenation reactor from an organic liquid hydride inlet at a flow rate of 25.16g/min, 2.51g/min N-ethylcarbazole and 0.91g/min hydrogen are generated in a dehydrogenation reaction zone, the N-ethylcarbazole slowly converges and flows out from an organic liquid outlet along with the progress of the reaction, the hydrogen rises to enter a gas-liquid separation zone, the temperature of the carried organic liquid is reduced when the hydrogen passes through a metal mesh with the thickness of 1cm, the carried organic liquid is condensed and adsorbed on the metal mesh and then drops into the dehydrogenation reaction zone, and the hydrogen continuously rises and flows out from the hydrogen outlet; the conversion of the dehydrogenation reaction was approximately 97% at a reaction temperature of 220 ℃. The method comprises the steps that a mixture of hydrogen and air enters a reactor from a mixed gas inlet at a flow rate of 116.44g/min, the mixed gas passes through a gas distribution area, the gas distribution area is filled with porous media with 98% of porosity, the porous media uniformly distributed and then enters a catalytic combustion area, the catalytic combustion area is filled with foam nickel with 90% of porosity as a matrix of a catalyst, the loading amount of carrier alumina is 10wt%, the loading amount of active component platinum is 1wt%, the mixed gas generates catalytic combustion reaction to emit heat to a heat pipe, the heat pipe transfers the heat to a dehydrogenation reaction area, the coupling of the dehydrogenation reaction and the catalytic combustion reaction is completed, 116.68g/min of combustion tail gas is discharged from a tail gas outlet through a collection area, and the hydrogen content is lower than 4%; the number of the heat pipes is 12, the heat pipes are arranged on the metal plate in a square shape, the length of the heat pipes is 70mm, the diameter of the heat pipes is 8mm, the heat pipes are made of copper, the working medium is water, and the liquid filling rate is 30%. The power generation efficiency of the fuel cell is 55%, the reactor can supply hydrogen for the fuel cell of 1kw and can supply heat by itself.
The embodiments described above are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the embodiments described above, and any other changes, modifications, alternative combinations and simplifications that do not depart from the spirit and principles of the present invention should be made in the equivalent manner, and are included in the scope of the present invention.
Claims (8)
1. The on-vehicle organic liquid hydride dehydrogenation reactor is characterized by comprising an upper dehydrogenation reaction zone and a lower catalytic combustion zone, wherein the dehydrogenation reaction zone and the catalytic combustion zone are isolated from each other;
the catalytic combustion zone is filled with a catalytic oxidation catalyst for hydrogen catalytic combustion reaction; the left side of the catalytic combustion zone is provided with a mixed gas distribution zone, and the right side of the catalytic combustion zone is provided with a tail gas collection zone; the mixed gas distribution area is used for uniformly distributing the mixed gas of hydrogen and oxygen; a heat pipe is vertically arranged in the catalytic combustion zone; the heat pipe penetrates through the catalytic combustion zone and the dehydrogenation reaction zone;
the catalytic oxidation catalyst consists of a catalyst matrix, a catalyst carrier and a catalyst active component; the catalyst matrix is an integral porous medium, the porosity of the porous medium is 85-95%, and the aperture is 0.5-2 mm; the catalyst carrier is a metal oxide loaded on a catalyst matrix, and the loading amount is 0.5-20wt%; the active component of the catalyst is noble metal loaded on a catalyst carrier, and the loading amount is 0.1-2 wt%;
the dehydrogenation reaction zone is arranged at the upper part of the catalytic combustion zone, and the dehydrogenation catalyst is filled in the dehydrogenation reaction zone; the upper part of the dehydrogenation reaction zone is provided with a gas-liquid separation zone, and the gas-liquid separation zone is provided with a metal net with the thickness of 1 cm-10 cm; the bottom of the metal net is 1 cm-5 cm away from the dehydrogenation reaction zone; the top of the gas-liquid separation zone is provided with a hydrogen outlet;
the dehydrogenation reaction zone is filled with an integral dehydrogenation catalyst, and the dehydrogenation catalyst is provided with a plurality of through holes for placing heat pipes; the dehydrogenation catalyst consists of a catalyst matrix, a catalyst carrier and a catalyst active component; the catalyst matrix is an integral porous medium, the porosity of the porous medium is 85% -98%, and the aperture of the porous medium is 1 mm-3 mm; the catalyst carrier is loaded on a catalyst substrate, and the loading capacity of the carrier is 1-20wt%; the catalyst active component is loaded on a catalyst carrier, and the loading amount of the active component is 0.1-20wt%;
the height of the dehydrogenation reaction zone is 1.1-1.5 times of the height of the catalytic combustion zone.
2. The reactor of claim 1, wherein the mixed gas distribution area has a horn-like structure with a cross section of isosceles trapezoid with a base angle of 60 to 90 °.
3. The reactor of claim 1, wherein the mixed gas distribution zone is filled with a porous medium having a porosity of 80% -98% and a pore size of 0.1 mm-1.5 mm.
4. The reactor of claim 1, wherein the catalytic oxidation catalyst packed in the catalytic combustion zone catalyzes the oxidation of hydrogen at 150 ℃ to 500 ℃.
5. The reactor according to claim 1, wherein the catalytic oxidation catalyst is further provided with an auxiliary agent, and the auxiliary agent is cerium oxide and/or zirconium oxide, and the loading amount is 1wt% -10 wt%.
6. The reactor of claim 1, wherein the working medium in the heat pipe is water and the pipe wall material is a metal material; the number of the heat pipes is set according to the size of the reactor, and the arrangement mode is one or the combination of more than one of regular triangle, corner triangle, regular square and corner regular square; the distance from the lower end of the heat pipe to the bottom of the reactor is more than or equal to 5mm, and the distance from the upper end of the heat pipe to the organic liquid outlet/organic liquid hydride inlet is more than or equal to 5mm.
7. The reactor according to claim 1, wherein the tail gas collecting area is of a horn-shaped structure, the section of the tail gas collecting area is in an isosceles trapezoid shape, and the bottom angle of the trapezoid is 60-90 degrees; and one end of the tail gas collecting area with smaller inner diameter is connected with a tail gas outlet.
8. The reactor of claim 1, wherein the dehydrogenation reaction zone and catalytic combustion zone are separated by a metal plate.
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