CN102502494B - Laminated type reactor for hydrogen production by reforming alcohols - Google Patents
Laminated type reactor for hydrogen production by reforming alcohols Download PDFInfo
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Abstract
The invention relates to a laminated type reactor for hydrogen production by reforming alcohols, belonging to the technical field of hydrogen energy sources and micro-machining. The laminated type reactor comprises a left end cover plate, a first heat exchanger, a reforming combustion room, a second heat exchanger and a right end cover plate. The left end cover is provided with an air inlet and a combustion material inlet. The first heat exchanger, the reforming combustion room and the second heat exchanger are sequentially overlapped and are placed between the left end cover plate and the right end cover plate. The first heat exchanger is composed of a plurality of separation plates and a plurality of heat exchange plates which are repeatedly and alternatively arrayed, and the second heat exchanger is composed of a plurality of the separation plates and a plurality of the heat exchange plates, and an oxidization plate, wherein the separation plates and the heat exchange plates are repeatedly and alternatively arrayed. The reforming combustion room is composed of a plurality of the separation plates and a plurality of reforming combustion plates, which are repeatedly and alternatively arrayed; and the right end cover plate is provided with a reforming material inlet, a reforming tail gas outlet and the like. By adopting a plate type multi-layer laminating technology, the laminated type reactor provided by the invention has the advantages of greatly-reduced equipment volume, simple structure, capability of being flexibly dismounted, easy machining of a plate type micro-structure, low machining cost and good equipment integration.
Description
Technical field
The present invention relates to a kind of stacked alcohol reforming hydrogen production reactor, belong to hydrogen energy source and micro-processing technology field.Belong to the hydrogen producing technology field.
Background technology
At present, the huge energy resource system of setting up in 20th century can't adapt to Future Society to the requirement of the energy system of efficient, cleaning, safety, and energy development is being faced with huge challenge.The production of the energy and consumption and global climate change have close relationship with tellurian Greenhouse effect.Therefore, improve the utilization ratio of the energy and the main themes that the development substitute energy will become 21 century.The above-mentioned pollutent of motor vehicle emission produces a very large impact HUMAN HEALTH, causes the severe contamination of environment.According to the statistics made by the departments concerned, automobile exhaust pollution accounts for 42% of topsoil.Therefore, research cleaning vehicle (zero-emission vehicle) has caused various countries scholar's extensive attention.It is reported, the total working efficiency of fuel cell will exceed about 1 times than traditional combustion engine, and without any pollutant emission.At present, the research and development of fuel cell technology is the attention of national governments and major company extremely, and the nineties in 20th century, Proton Exchange Membrane Fuel Cells (PEMFC) technology has obtained high speed development.In 21 century, Proton Exchange Membrane Fuel Cells will move towards rapidly to use, and becomes new industry.The optimum feed stock of fuel cell is hydrogen, and since fuel cell is born, hydrogen supply and fuel cell itself all is the core technology of no less important.The PEMFC hydrogen source technology has two classes at present: the one, and fuel cell carries pure hydrogen; The 2nd, the on-the-spot hydrogen manufacturing of liquid fuel.Because pure hydrogen price is high, poor stability, conveying store and the filling difficulty, limited the sizable application of fuel cell.The on-the-spot hydrogen producing technology of liquid phase alcohols, hydrocarbon reformation has that energy density is high, effciency of energy transfer is high, liquid fuel easily transports, replenishes and stores, also having advantage clearly at aspects such as economy, securities, is the hydrogen energy source technology of the most real fuel cell.Fuel cell will be applied to portable power source, and the hydrogen manufacturing fuel processing system must satisfy that volume is little, quality is light, startup and the load responding time is short, reliability is high and cost is low particular requirement, and is unpractical with the fuel reforming system miniaturization of conventional yardstick.The hydrogen manufacturing fuel processing system is introduced in the microchannel, not only can reduce volume and the quality of reactive system, can also optimize complicated reaction process, improve reaction efficiency.Technology is introduced in microchannel with respect to other, and sheet lamination technology is incorporated in the parts thermo-negative reaction and thermopositive reaction becomes possibility, has not only saved the space, has also strengthened the recycle of energy, has reduced thermosteresis.
Application number is methanol self-heating reforming hydrogen making integrated apparatus and the hydrogen production process that the Chinese invention patent of 200710159028.X discloses a kind of microminiaturization.It is introduced integrated system and is comprised of four module: one group of methanol self-heating recapitalization/heat exchange module; One group of catalyticcombustion/vaporization module, two groups of CO selective oxidation/heat exchange modules, four pack modules are monoblock type catalyticreactor and micro-channel heat exchanger welding integration mode.But because the large multi-part of this reactor is welding process, so inconvenient dismounting forms, little processing mode is the chemical etching technology, and cost is higher.
Application number is that 200910100100.0 Chinese invention patents disclose a kind of self-heating type alcohol reforming hydrogen production micro passage reaction with the micro-boss array architecture.The self-heating system that its is introduced is comprised of the stack of three ply board shape reaction carriers, and all with the micro-boss structure, levels is single face micro-boss array on three layers, and the centre is two-sided micro-boss array.Three stacked two chambers of rear formation that add, the upper strata is the catalytic reforming passage, lower floor is combustion channels.This invention has increased the specific volume of reactor, has improved the productive rate of reformation hydrogen production.But this structure of reactor is more single, and the heat exchange aspect does not have emphasis to consider, the assembling of simultaneous reactions device needs diffusion welding process repeatedly, and assembling is inconvenient, and the reactor of welding can bring again very large difficulty for dismounting.
Summary of the invention
The present invention seeks to propose a kind of stacked alcohol reforming hydrogen production reactor, make reactor can realize that heat exchange, reformation, burning, four steps of CO selective oxidation move simultaneously, can guarantee again not clash between the several functions, reactor belongs to the self-heating operational mode, need not outside heat under the running status.
The stacked alcohol reforming hydrogen production reactor that the present invention proposes comprises left end cover plate, First Heat Exchanger, reforming combustion chamber, the second interchanger and right-hand member cover plate; Have an air intlet and a burning material inlet on the described left end cover plate; Described First Heat Exchanger, reforming combustion chamber and the second interchanger be overlapping being placed between left end cover plate and the right-hand member cover plate successively; Described First Heat Exchanger is comprised of a plurality of dividing plates and a plurality of heat exchanger plates, and a plurality of dividing plates and a plurality of heat exchanger plates repeat alternative arrangement; Described the second interchanger is comprised of a plurality of dividing plates, a plurality of heat exchanger plates and an oxidation plate, and a plurality of dividing plates and a plurality of heat exchanger plates repeat alternative arrangement, and described oxidation plate is replaced in a plurality of heat exchanger plates; Described reforming combustion chamber is comprised of a plurality of dividing plates and a plurality of reforming combustion plate, and a plurality of dividing plates and a plurality of reforming combustion plate repeat alternative arrangement; Have a reformation material inlet, a reformation tail gas outlet, a combustion tail gas outlet and an air intlet on the described right-hand member cover plate.
In the above-mentioned reactor, the middle part in the front of described heat exchanger plates is provided with many group cold fluid pass, form serpentine flow by the baffling groove between every two adjacent groups cold fluid pass, one end of serpentine flow is provided with the cold fluid import, the serpentine flow the other end relative with the cold fluid import has the cold fluid outlet, the inboard has gas passage around the serpentine flow, and the outside has bolt slot; The middle part of heat exchanger plates reverse side is provided with zone of heat liberation, and an end of zone of heat liberation is provided with the hot-fluid import, and the zone of heat liberation the other end relative with the hot-fluid import has the hot-fluid outlet.
In the above-mentioned reactor, the positive middle part of described reforming combustion plate is provided with the combustioncatalysts rest area, the relative both sides of combustioncatalysts rest area have burning gas import and combustion tail gas outlet, one side of burning gas import has one group of air inlet port, inboard around the combustioncatalysts rest area has gas passage, the gas passage opposite end has reformed gas import and the outlet of reformation tail gas, and the outside has bolt slot; The middle part of the reverse side of reforming combustion plate is provided with the reforming catalyst rest area, and the relative both sides of reforming catalyst rest area have reformed gas import and the outlet of reformation tail gas, and an end of gas passage is provided with the gas stream groove, and this gas stream groove and air inlet port link.
In the above-mentioned reactor, the positive middle part of described oxidation plate is provided with the oxide catalyst rest area, one end of oxide catalyst rest area is provided with the import of reformation tail gas, one side of reformation tail gas import has one group of air inlet port, the oxide catalyst rest area the other end relative with the import of reformation tail gas has the outlet of reformation tail gas, inboard around the oxide catalyst rest area has gas passage, and an end of one of them gas passage has the cold fluid import, and the outside has bolt slot; The middle part of the reverse side of oxidation plate is provided with cold fluid pass, and an end of cold fluid pass is provided with the gas stream groove, and this gas stream groove and air inlet port link.
The stacked alcohol reforming hydrogen production reactor that the present invention proposes, its characteristics and advantage are:
1, reforming hydrogen-preparation reactor of the present invention adopts board-like multi-layer stacks technology, so that the module of several functions can organically be grouped together, greatly reduced the volume of equipment, and simple in structure, flexibly dismounting, board-like lamination mode easier scale are amplified, and the microstructure handling ease realizes, tooling cost is low, and equipment integration is functional;
2, reforming hydrogen-preparation reactor of the present invention, owing to having adopted the lamination mode, the heat transfer process of reforming and burning is accelerated greatly, be alternately distributed so that the heat distribution of reformer chamber plane is more even, heat transfer efficiency in the interchanger obviously improves, heat transfer process is mostly transmitted in metal, so that heat transfer rate is accelerated greatly, start time is shorter;
3, the introducing of microchannel on the lamination of reforming hydrogen-preparation reactor of the present invention so that resistance to heat obviously descends between wall, has improved the feasibility of self-heating operation, simultaneously so that the security of reaction significantly improve;
Thermal coupling problem during 4, according to reformation, burning, reforming hydrogen-preparation reactor of the present invention has taken into full account the reasonable utilization of internal heat, and the interchanger that distributes to reach minimum thermosteresis, has been realized good coupling between heat release, heat absorption, condensation, the vaporization.
Description of drawings
Fig. 1 is the structural representation of the stacked alcohol reforming hydrogen production reactor that proposes of the present invention.
Fig. 2 is the wiring layout of the stacked alcohol reforming hydrogen production reactor of the present invention.
Fig. 3 is each arrangements of components schematic diagram in the First Heat Exchanger of the stacked alcohol reforming hydrogen production reactor of the present invention.
Fig. 4 is heat exchanger plates Facad structure schematic diagram in the interchanger of the stacked alcohol reforming hydrogen production reactor of the present invention.
Fig. 5 is the reverse side structural representation of heat exchanger plates shown in Figure 4.
Fig. 6 is each arrangements of components schematic diagram in the reforming combustion chamber of the stacked alcohol reforming hydrogen production reactor of the present invention.
Fig. 7 is the Facad structure schematic diagram of reforming combustion plate in the stacked alcohol reforming hydrogen production reactor of the present invention.
Fig. 8 is the reverse side structural representation of reforming combustion plate shown in Figure 7.
Fig. 9 is each arrangements of components schematic diagram in the second interchanger of the stacked alcohol reforming hydrogen production reactor of the present invention.
Figure 10 is the Facad structure schematic diagram of oxidation plate in the second interchanger.
Figure 11 is the reverse side structural representation of oxidation plate shown in Figure 10.
Figure 12 is the principle of work schematic diagram of reactor of the present invention.
Figure 13 and Figure 14 are the effect schematic diagram of reactor of the present invention.
Among Fig. 1～Figure 12,1 is the left end cover plate, and 2 is First Heat Exchanger, 3 are the reformation combustion chamber, and 4 is the second interchanger, and 5 is the right-hand member cover plate, 6 is air intlet, and 7 are the burning material inlet, and 8 are the reformation material inlet, 9 are the outlet of reformation tail gas, 10 are the combustion tail gas outlet, and 11 is air intlet, and 12 is little pilot hole, 13 is large pilot hole, 14 is bolt slot, and 15 is gas passage, and 16 is dividing plate, 17 is heat exchanger plates, 18 is cold fluid pass, and 19 is the baffling groove, and 20 is the cold fluid import, 21 are the cold fluid outlet, 22 is the hot-fluid import, and 23 are the hot-fluid outlet, and 24 is zone of heat liberation, 25 are the reformation burner plate, 26 is the combustioncatalysts rest area, and 27 is the burning gas import, and 28 is air inlet port, 29 are the combustion tail gas outlet, 30 is the reformed gas import, and 31 are the outlet of reformation tail gas, and 32 is the reforming catalyst rest area, 33 is the gas stream groove, 34 are the oxidation plate, and 35 is the oxide catalyst rest area, and 36 are the import of reformation tail gas, 37 is air inlet port, 38 are the outlet of reformation tail gas, and 39 is the cold fluid import, and 40 are the cold fluid outlet, 41 is cold fluid pass, and 42 is the gas stream groove.
"+" and "-" among the figure are representing fluid flow direction, the flow direction that "+" representing liquid perpendicular to paper inwards, it is outside perpendicular to paper that "-" representing the flow direction of liquid.
Specific implementation method
The stacked alcohol reforming hydrogen production reactor that the present invention proposes, its structure comprises left end cover plate 1, First Heat Exchanger 2, reforming combustion chamber 3, the second interchanger 4 and right-hand member cover plate 5 as shown in Figure 1; Have an air intlet 6 and a burning material inlet 7 on the described left end cover plate 1; Described First Heat Exchanger 2, reforming combustion chamber 3 and the second interchanger 4 be overlapping being placed between left end cover plate 1 and the right-hand member cover plate 5 successively; Described First Heat Exchanger 2 is comprised of a plurality of dividing plates 16 and a plurality of heat exchanger plates 17, and a plurality of dividing plates 16 and a plurality of heat exchanger plates 17 repeat alternative arrangement; Described the second interchanger 4 is comprised of a plurality of dividing plates 16, a plurality of heat exchanger plates 17 and an oxidation plate 34, and a plurality of dividing plates 16 and a plurality of heat exchanger plates 17 repeats alternative arrangements, in a plurality of heat exchanger plates 17 of described oxidation plate 34 displacements one; Described reforming combustion chamber 3 is comprised of a plurality of dividing plates 16 and a plurality of reforming combustion plate 25, and a plurality of dividing plates 16 and a plurality of reforming combustion plate 25 repeat alternative arrangement; Have a reformation material inlet 8,10 and air intlets 11 of 9, combustion tail gas outlets of a reformation tail gas outlet on the described right-hand member cover plate 5.
In the stacked alcohol reforming hydrogen production reactor that the present invention proposes, the structure of First Heat Exchanger 2 as shown in Figure 3, repeating alternative arrangement by a plurality of dividing plates 16 and a plurality of heat exchanger plates 17 forms, export 23 relative position by dividing plate 16 and change cold fluid import 20, cold fluid outlet 21, hot-fluid import 22, hot-fluid, realize that cold and hot fluid is in First Heat Exchanger 1 interior different spaces countercurrent flow, cold and hot fluid is passed through all heat exchanger plates 17 successively simultaneously, and is mutually non-cross.
The structure of the heat exchanger plates in the above-mentioned First Heat Exchanger, as shown in Figure 4 and Figure 5, Figure 4 shows that the front of heat exchanger plates 17, its middle part is provided with many group cold fluid pass 18, form serpentine flow by baffling groove 19 between every two adjacent groups cold fluid pass 18, an end of serpentine flow is provided with cold fluid import 20, has cold fluid outlet 21 with the cold fluid import 20 relative serpentine flow the other ends, the inboard has gas passage 15 around the serpentine flow, and the outside has bolt slot 14.Figure 5 shows that the reverse side of heat exchanger plates 17, its middle part is provided with zone of heat liberation 24, and an end of zone of heat liberation 24 is provided with hot-fluid import 22, has hot-fluid outlet 23 with hot-fluid import 22 relative zone of heat liberation 24 the other ends.
In the stacked alcohol reforming hydrogen production reactor that the present invention proposes, the structure of reforming combustion chamber as shown in Figure 6, reforming combustion chamber 3 is repeated alternative arrangement by a plurality of dividing plates 16 and a plurality of reforming combustion plate 25 and is formed, stack by dividing plate 16 and reforming combustion plate 25, realize that reforming reaction and combustion reactions react in differential responses chambers 3, reforming combustion chamber, simultaneously two kinds of fluid countercurrent flows, reformation, combustible fluid are simultaneously by all reforming combustion plates 25, and are mutually non-cross.
The structure of reforming combustion plate 25 as shown in Figure 7 and Figure 8 in the above-mentioned reforming combustion chamber, Figure 7 shows that the front of reforming combustion plate 25, its middle part is provided with combustioncatalysts rest area 26, the relative both sides of combustioncatalysts rest area 26 have 27 burning gas imports and the outlet of 29 combustion tail gas, one side of burning gas import 27 has one group of air inlet port 28, inboard around the combustioncatalysts rest area 26 has gas passage 15, gas passage 15 opposite ends have reformed gas import 30 and reformation tail gas outlet 31, and the outside has bolt slot 14; Figure 8 shows that the reverse side of reforming combustion plate 25, its middle part is provided with reforming catalyst rest area 32, reforming catalyst rest area 32 relative both sides have reformed gas import 30 and reformation tail gas outlet 31, one end of gas passage 14 is provided with gas stream groove 33, and this gas stream groove 33 links with air inlet port 28.
The second interchanger in the stacked alcohol reforming hydrogen production reactor that the present invention proposes, its structure as shown in Figure 9, the second interchanger 4 repeats alternative arrangements by a plurality of dividing plates 16, a plurality of heat exchanger plates 17 and an oxidation plate 34 and forms, in a plurality of heat exchanger plates 17 of described oxidation plate 34 displacements one; Export 23 relative position by dividing plate 16 and change cold fluid import 20, cold fluid outlet 21, hot-fluid import 22, hot-fluid, realize that cold and hot fluid is in First Heat Exchanger 1 interior different spaces countercurrent flow, cold and hot fluid is passed through all heat exchanger plates 17 successively simultaneously, and is mutually non-cross.
The structure of the heat exchanger plates in above-mentioned the second interchanger as shown in Figure 10 and Figure 11, Figure 10 shows that the front of oxidation plate 34, its middle part is provided with oxide catalyst rest area 35, one end of oxide catalyst rest area 35 is provided with reformation tail gas import 36, one side of reformation tail gas import 36 has one group of air inlet port 37, oxide catalyst rest area 35 the other ends relative with reformation tail gas import 36 have reformation tail gas outlet 38, inboard around the oxide catalyst rest area 35 has gas passage 15, one end of one of them gas passage 15 has cold fluid import 39, and the outside has bolt slot 14; Figure 11 shows that the reverse side of oxidation plate 34, its middle part is provided with cold fluid pass 41, and an end of cold fluid pass 41 is provided with gas stream groove 42, and this gas stream groove and air inlet port link.
Below in conjunction with Figure 12, introduce in detail the principle of work of reactor of the present invention:
The cold fluid import 20 in heat exchanger plates 17 fronts links in burning material inlet 7 on the left end cover plate 1 and the First Heat Exchanger 2, the burning material carries out heat exchange by the hot-fluid in the zone of heat liberation 24 of many groups cold fluid pass 18 and heat exchanger plates 17 reverse side, flowed out by cold fluid outlet 21 after the heat absorption, cold fluid import 20 by next piece heat exchanger plates 17 front enters second heat exchanger plates, repeat endothermic process, until flowed out by last piece heat exchanger plates 17 front cold fluid outlets 21, obtain the vaporizing burning material of rear certain temperature, the good burning material of vaporization is entered in all reforming combustion plates 25 simultaneously by the burning gas import 27 in reforming combustion plate 25 fronts; Air is entered by the air intlet 6 on the left end cover plate 1, by the gas passage in First Heat Exchanger 2 and the reforming combustion chamber 3, enter combustioncatalysts rest area 26 and the good burning mixing of materials of gasification via gas stream groove 33 via air inlet port 28, be provided with the combustioncatalysts of combustioncatalysts rest area 26 by reforming combustion plate 25 positive middle parts, combustion reactions heat release afterfire tail gas occur flowed out by combustion tail gas outlet 29; Combustion tail gas enters in the second interchanger 4 through the hot-fluid import 22 in first heat exchanger plates 17 front in the second interchanger 4, carry out heat exchange with First Heat Exchanger 2 same principles, hot-fluid outlet 23 by last piece heat exchanger plates 17 reverse side in the second interchanger exports 10 outflow reactors by the combustion tail gas on the right-hand member cover plate.Equally, the cold fluid import 20 in heat exchanger plates 17 fronts links in reformation material inlet 8 on the described right-hand member cover plate 5 and the second interchanger 4, the reformation material is by the second interchanger heat absorption vaporization, vaporization reformation material is well entered in all reforming combustion plates 25 simultaneously by the reformed gas import 30 of reforming combustion plate 25 reverse side, be provided with the reforming catalyst of reforming catalyst rest area 26 by reforming combustion plate 25 reverse side middle part, reformation tail gas is flowed out by reformation tail gas outlet 31 behind the generation endothermic reforming reaction; The hot-fluid import 22 of last piece heat exchanger plates 17 reverse side enters and carries out heat exchange in the First Heat Exchanger 2 in the reformation tail gas process First Heat Exchanger 2.
In the present invention, oxidation plate 34 Main Functions in the second interchanger 3 are to make CO carry out selective oxidation.
In the stacked alcohol reforming hydrogen production reactor of the present invention, the catalyzer of reformation, burning, CO selective oxidation can adopt the modes such as foamed metal monolith catalyzers, direct metal wall carried catalyst, beaded catalyst, honeycomb substrate catalyzer.This experiment test catalyst reactor is foamed metal load integer catalyzer, and this mode catalyst utilization is high, can greatly improve hydrogen yield.
Stacked alcohol reforming hydrogen production reactor of the present invention, wherein Micro Channel Architecture processing can be adopted the mode of numerical control micromachined, and cost is lower.
In the stacked alcohol reforming hydrogen production reactor of the present invention, entry of combustion chamber and reformer chamber entrance and CO selective oxidation chamber inlet have carbon fiber paper or silica wool weighting material, make material be evenly distributed to obtain equally distributed temperature of reaction, prevent that granules of catalyst from entering in the interchanger.
This reactor adopts the mode of mechanical seal, adds flexible graphite gasket between lamination, by bolted pressure sealing on two side cover plates, and the operations such as this mode easy disassembly, maintenance, replacing parts.
Stacked alcohol reforming hydrogen production reactor of the present invention, reforming reaction such as alcohol steam reformed hydrogen-producing reaction formula are:
12C
2H
5OH+12H
2O=26H
2+ 11CH
4+ 11CO
2+ 2CO Δ H＞0 is endothermic process, and temperature of reaction is between 300 ℃-375 ℃.Combustion reactions is that ethanol direct oxidation combustion reactions formula is:
C
2H
5OH+2O
2=3H
2O+2CO
2Δ H＜0 is exothermic process, and the burning heat release provides heat for reforming reaction.
The assembling flow path of stacked alcohol reforming hydrogen production reactor of the present invention is: 1) supporting of catalyzer: the nickel foam that 2.5mm is thick cuts into reaction chamber size first, oil removing, mild acid wash, washing post-drying.The catalyzer for preparing is added organic solvent make viscous paste, be immersed on the porous nickel mesh, repeated impregnations post-drying repeatedly, 450 ℃ of burnings obtain monolithic catalyst; 2) assembling of lamination: add flexible graphite gasket between each lamination sheets, utilize 12 bolted compacting sealings on the two end cover plate; 3) the outside connection: be welded with the stainless steel connecting joint on the two end cover plate, connect the stainless steel pipeline of Φ 3 by cutting ferrule, external pumping unit.Wherein insert respectively thermopair, external temperature operating device in the reformation-burner plate; 4) each several part value: the reforming catalyst consumption is: 20g; The combustioncatalysts consumption is: 20g; CO catalyst for selective oxidation consumption is: 10g; The final consumption of reformation solution is: ethanol 12.96mol/h and water 38.88mol/h; The final consumption of burning ethanol is: ethanol is that 0.81mol/h and air are 38.52mol/h; CO selective oxidation air consumption is: 5.2mol/h.
Stacked alcohol reforming hydrogen production reactor of the present invention, its schedule of operation is: at first utilize the metal electric heating piece, to reform-chamber temperature is preheating between 250 ℃-300 ℃, then enter the heat release of burning in the combustion reactor after by pump 1 ethanol being passed through First Heat Exchanger and the air mixed by pump 2, system's reformation-chamber temperature is risen to reform temperature required about 360 ℃.After temperature reaches, by pump 3 ethanol-water solution is entered heat absorption reformation in the reforming reactor through the second interchanger.Make system stable operation by the software control self-heating temperature behind the system stability.Concrete combustion reactions formula is as follows:
Combustion reactions: C
2H
5OH+2O
2=3H
2O+2CO
2
Exothermic heat of reaction: Δ H=-1272.2kj/mol (360 ℃)
The reaction formula that reforming reaction obtains the corresponding chemical metering by experiment is:
Reforming reaction: 12C
2H
5OH+12H
2O=26H
2+ 11CH
4+ 11CO
2+ 2CO
Endothermic heat of reaction: Δ H=39.75kj/mol (350 ℃)
CO selective oxidation: 2CO+O
2=2CO
2Heat release is: Δ H=-275.3kj/mol (220 ℃)
Be the small-sized hydrogen making machine of 1KW power according to experimental design.In the experiment, this hydrogen making machine can produce reformed gas flow 1.2KL/h, and wherein, hydrogen content is more than 60%, and the CO content decrease is the 100ppm level, satisfies the fuel cell service requirements, and gas space velocity is 2000/h, illustrates that this system can meet design requirement.
Figure 13 is 2000 hour life-span of reforming hydrogen-preparation reactor reforming catalyst of the present invention, selectivity test result.Under 350 ℃ of steady temperatures, to Ni/CeO
2Catalyzer has carried out stability test.(mol ratio is H to aqueous ethanolic solution
2O: C
2H
5OH=3: 1) speed with 0.05ml/min enters vaporizer, flows into fixed-bed reactor after vaporizing and reforms, and enters Agilent 7890A type gas chromatograph after the process condensation of outlet product and the drying and carries out proximate analysis.
Figure 14 is that reforming hydrogen-preparation reactor reforming catalyst of the present invention starts the selectivity test result 12 times.To NiCrZnCu/CeO
2Catalyzer has carried out reperformance test.Aqueous ethanolic solution (H
2O: C
2H
5OH=3: 1 mol ratio) speed with 0.05ml/min enters vaporizer, flows into fixed-bed reactor after vaporizing and reforms, and enters Agilent 7890A type gas chromatograph after the process condensation of outlet product and the drying and carries out proximate analysis.
Claims (4)
1. a stacked alcohol reforming hydrogen production reactor is characterized in that this reactor comprises left end cover plate, First Heat Exchanger, reforming combustion chamber, the second interchanger and right-hand member cover plate; Have an air intlet and a burning material inlet on the described left end cover plate; Described First Heat Exchanger, reforming combustion chamber and the second interchanger be overlapping being placed between left end cover plate and the right-hand member cover plate successively; Described First Heat Exchanger is comprised of a plurality of dividing plates and a plurality of heat exchanger plates, and a plurality of dividing plates and a plurality of heat exchanger plates repeat alternative arrangement; Described the second interchanger is comprised of a plurality of dividing plates, a plurality of heat exchanger plates and an oxidation plate, and a plurality of dividing plates and a plurality of heat exchanger plates repeat alternative arrangement, and described oxidation plate is replaced in a plurality of heat exchanger plates; Described reforming combustion chamber is comprised of a plurality of dividing plates and a plurality of reforming combustion plate, and a plurality of dividing plates and a plurality of reforming combustion plate repeat alternative arrangement; Have a reformation material inlet, a reformation tail gas outlet, a combustion tail gas outlet and an air intlet on the described right-hand member cover plate.
2. reactor as claimed in claim 1, the middle part that it is characterized in that the front of wherein said heat exchanger plates is provided with many group cold fluid pass, form serpentine flow by the baffling groove between every two adjacent groups cold fluid pass, one end of serpentine flow is provided with the cold fluid import, the serpentine flow the other end relative with the cold fluid import has the cold fluid outlet, the inboard has gas passage around the serpentine flow, and the outside has bolt slot; The middle part of heat exchanger plates reverse side is provided with zone of heat liberation, and an end of zone of heat liberation is provided with the hot-fluid import, and the zone of heat liberation the other end relative with the hot-fluid import has the hot-fluid outlet.
3. reactor as claimed in claim 1, the positive middle part that it is characterized in that wherein said reforming combustion plate is provided with the combustioncatalysts rest area, the relative both sides of combustioncatalysts rest area have burning gas import and combustion tail gas outlet, one side of burning gas import has one group of air inlet port, inboard around the combustioncatalysts rest area has gas passage, the gas passage opposite end has reformed gas import and the outlet of reformation tail gas, and the outside has bolt slot; The middle part of the reverse side of reforming combustion plate is provided with the reforming catalyst rest area, and the relative both sides of reforming catalyst rest area have reformed gas import and the outlet of reformation tail gas, and an end of gas passage is provided with the gas stream groove, and this gas stream groove and air inlet port link.
4. reactor as claimed in claim 1, the positive middle part that it is characterized in that wherein said oxidation plate is provided with the oxide catalyst rest area, one end of oxide catalyst rest area is provided with the import of reformation tail gas, one side of reformation tail gas import has one group of air inlet port, the oxide catalyst rest area the other end relative with the import of reformation tail gas has the outlet of reformation tail gas, inboard around the oxide catalyst rest area has gas passage, one end of one of them gas passage has the cold fluid import, and the outside has bolt slot; The middle part of the reverse side of oxidation plate is provided with cold fluid pass, and an end of cold fluid pass is provided with the gas stream groove, and this gas stream groove and air inlet port link.
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| CN103418321B (en) * | 2013-08-19 | 2014-12-17 | 浙江大学 | Layered micro-channel reactor with uniformly distributed micro-channel flow velocities |
| CN106586957A (en) * | 2015-10-17 | 2017-04-26 | 深圳伊腾迪新能源有限公司 | Laminated reforming hydrogen producer |
| CN107583577B (en) * | 2017-11-01 | 2019-12-06 | 临沂大学 | method for carrying out adsorption-desorption thermal coupling reaction by using micro-reaction system |
| CN109956449B (en) * | 2017-12-14 | 2022-07-26 | 中国科学院大连化学物理研究所 | Parallel flow type methanol-water reforming hydrogen production reactor |
| CN111326772B (en) * | 2018-12-14 | 2022-03-04 | 中国科学院大连化学物理研究所 | Fuel cell system based on broad-spectrum fuel and operation method thereof |
| CN110420644A (en) * | 2019-08-16 | 2019-11-08 | 广西氢朝能源科技有限公司 | A kind of production method of palladium membrane component and its application in hydrogen from methyl alcohol reactor |
| CN112999986A (en) * | 2021-04-21 | 2021-06-22 | 广东蓝玖新能源科技有限公司 | Plate type reactor |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2668600Y (en) * | 2003-07-11 | 2005-01-05 | 华东理工大学 | Plate-fin type methanol vapour reforming hydrogen-making system |
| CN1629065A (en) * | 2003-12-16 | 2005-06-22 | 中国科学院大连化学物理研究所 | Microchannel plate-fin type water vapour reforming reactor for hydrogen production |
| CN101462694A (en) * | 2007-12-19 | 2009-06-24 | 中国科学院大连化学物理研究所 | Miniaturized methanol self-heating reforming hydrogen making integrated apparatus and hydrogen production method |
| CN202346756U (en) * | 2011-11-04 | 2012-07-25 | 中国人民解放军防化指挥工程学院 | Laminated type alcohol reforming hydrogen production reactor |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05105404A (en) * | 1991-10-21 | 1993-04-27 | Ishikawajima Harima Heavy Ind Co Ltd | Plate type reformer |
-
2011
- 2011-11-04 CN CN 201110346279 patent/CN102502494B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2668600Y (en) * | 2003-07-11 | 2005-01-05 | 华东理工大学 | Plate-fin type methanol vapour reforming hydrogen-making system |
| CN1629065A (en) * | 2003-12-16 | 2005-06-22 | 中国科学院大连化学物理研究所 | Microchannel plate-fin type water vapour reforming reactor for hydrogen production |
| CN101462694A (en) * | 2007-12-19 | 2009-06-24 | 中国科学院大连化学物理研究所 | Miniaturized methanol self-heating reforming hydrogen making integrated apparatus and hydrogen production method |
| CN202346756U (en) * | 2011-11-04 | 2012-07-25 | 中国人民解放军防化指挥工程学院 | Laminated type alcohol reforming hydrogen production reactor |
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