CN1629065A - Microchannel plate-fin type water vapour reforming reactor for hydrogen production - Google Patents
Microchannel plate-fin type water vapour reforming reactor for hydrogen production Download PDFInfo
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Abstract
The invention discloses a microchannel plate-fin type water vapour reforming reactor for hydrogen production, wherein the main unit is a microchannel plate-fin structure, with a plurality of sealing heads through soldering, the reactor consists two combustion chambers, a reforming chamber and two gasification chambers, whereint he hydrogen-rich gas and air are subject to catalytic combustion reaction in the combustion chamber, discharging a vast amount of heat, which is transferred to the reforming chamber and the two gasfication chambers through a heat guide board, the raw material liquid first enters the two gasification chambers of the hydrogen production reactor, then enters the reforming chamber after being gasified, finally is reformed in the reforming chamber to obtain gaseous mixture of hydrogen gas that meets requirement.
Description
Technical field
The present invention relates to the hydrogen producer technical field, is a kind of microchannel plate-fin steam reforming hydrogen manufacturing reactor, and reforming hydrogen-preparation reactor is the core of whole hydrogen source system.The invention particularly relates to (1～1000NM on a small scale
3/ hr) fixedly hydrogen source device and vehicle-mounted onboard hydrogen source system provide the reactor of hydrogen source for fuel cell.
Background technology
The energy is most important key element in the economical activities of mankind.As everyone knows, the world today is being faced with problems such as the serious day by day and Greenhouse effect of energy shortage, environmental pollution, and in order to protect the environment that the mankind depend on for existence and to make sustained economic development, the clean new and renewable sources of energy of exploitation has been extremely urgent.Many countries, especially a lot of developed countries with the Hydrogen Energy of cleaning as oneself future source of energy and step up to research and develop.Hydrogen Energy is as a kind of renewable energy source of cleaning, has again simultaneously to store up the characteristics that can fail, and in the long term, its development may bring the great change of energy structure, thereby causes " hydrogen economy ", promptly is the politics that drives of the energy and economic with hydrogen.It is politics, the military conflict of purpose that the realization of hydrogen economy can reduce or eliminate with the contention oil, helps world peace.Therefore, research and develop Hydrogen Energy still all has particularly important to the Sustainable development of China to All Around The World meaning energetically.
What the fixed-bed reactor of current reformation hydrogen production generally adopted is the cylinder shell and tube, though this reactor is made simply, aspect the raising response capacity certain limitation is being arranged.Improving response capacity is exactly the loadings of considering how to improve heat interchanging area and catalyzer, for this drum type brake fixed-bed reactor, the general method that improves response capacity is exactly the loadings that the diameter of increasing tubulation or the quantity that increases tubulation improve the heat interchanging area and the catalyzer of reactor, will produce the inhomogeneous of radial temperature profile like this, cause reacting wayward, and can increase the generation of side reaction; If change the height that increases fixed-bed reactor into, what will occur like this that axial temperature distributes is inhomogeneous, thereby the transformation efficiency that causes reacting reduces, selectivity reduces and the energy efficiency of hydrogen manufacturing reduces.In addition, when the power requirement height arrived to a certain degree, this cylinder shell and tube reactor volume was bigger, and axial and radially bigger temperature head will cause system capacity efficient to reduce, even make the hydrogen production reaction in the reactor normally to carry out.
(patent No. US 6 for a patent of the U.S., 190,624 B1) also once introduced a kind of plate-type reactor of form, the structure that in this plate-type reactor, has added the plate wing, it is mainly used in a side generation chemical reaction, opposite side utilizes heat that fluid removal reaction emits with reaching the preheating fluidic simultaneously, takes away a large amount of heat of being emitted by reaction; Or utilize high temperature fluid to provide thermal source for reaction chamber; In addition, the plate fin structure in its reactor is in the downstream portion perforate, same fluid can be earlier through first chamber and be preheated (perhaps providing thermal source), after another chamber exothermic heat of reaction (or heat absorption) for the opposite side reaction.But the filling method of catalyzer is very complicated in this patent.
Summary of the invention
Technical problem to be solved by this invention is: the ununiformity of one, improving traditional cylinder calandria type fixed bed reactor temperature distribution; Two, improve the immiscibility that traditional shell and tube reactor internal flows distributes; Three, simplify structure of reactor, reduce the volume of reaction system, make it can satisfy on a small scale the fixedly needs of hydrogen source and onboard hydrogen source; Four, reduce to reform heat transmission resistance between heat absorption and the burning heat release improves heat-transfer effect, reaction efficiency and reaction preference; Five, improve the energy efficiency of system.
In order to address the above problem, the technical solution used in the present invention is: one, utilize gas distributor to make that material distributes more even in reaction chamber, and employing porous plate-fin structure, fluid can also mix in reaction chamber fully, overcome shell and tube reactor limitation in this respect, the raising of heat transfer efficiency simultaneously also makes structure of reactor more compact, and volume is less, has avoided owing to radially or axially growing the temperature distributing disproportionation that brings; Two, the major portion of whole reactor adopts the microchannel plate-fin structure, integrates preheating gasification, reformation, catalyst combustion reaction, has reduced the volume of reactor greatly; Three, utilize the mutual arrangement of reformation chamber and burning chamber position, rationally utilize the inside reactor heat, realized preferably the heat coupling between thermopositive reaction and thermo-negative reaction, vaporization and the reaction, increased heat-transfer effect, raising transformation efficiency and purpose optionally thereby reach.Be exactly specifically: one, all have only the heat transfer dividing plate of 0.4mm to be separated by between gasification chamber, burning chamber and the reformation chamber, and the heat transfer efficiency of microchannel plate fin structure itself just is better than shell and tube heat exchanger and plate-type heat exchanger greatly, gasify in addition, reformation, combustion reactions organically be combined in the plate-fin reactor, the volume of reactor is much smaller than the plate-type reactor of drum type brake fixed-bed reactor, shell and tube reactor and the slab construction of equal-wattage; Two, the reformation chamber is being clipped in the middle of two burning chambers, between them by heat-conducting plate heat conduction; Reformed gas and burning gas keep cross-flow on flow direction, the outside of two burning chambers is a gasification chamber, and reaction mass is first by entering the reformation chamber behind the gasification chamber of the outside again, and reaction mass is gas by gasification before entering the reformation chamber, make reforming reaction rapid, start time is shorter.
Specifically, the invention provides a kind of microchannel plate-fin steam reforming hydrogen manufacturing reactor, main part is the microchannel plate fin structure, adding several end sockets is welded, it has two burning chambers, and a reformation chamber and two gasification chambers are formed, and all have heat-conducting plate to be separated by between chamber and the chamber; Reformation chamber of two burning chamber therebetween, respectively there is a gasification chamber in the outside of two burning chambers; Respectively there is an end socket at the two ends of two burning chambers, and right-hand member end socket right side is provided with inlet mouth, and left end is a detachable end socket, on its lower wall, vertically are provided with the air outlet, are provided with snakelike heat exchange coil in the left end end socket; Also respectively there is an end socket at the two ends of reformation chamber and two gasification chambers, the left end of reformation chamber and two gasification chambers communicates through left end socket, right-hand member is after dividing plate is isolated, the right-hand member of two gasification chambers communicates with right end socket by feed distributor, and communicate with the inlet mouth on the right wall of right end socket, the right-hand member in reformation chamber communicates by the air outlet on the right wall of pipeline and right end socket; During work, catalyst combustion reaction takes place in the hydrogen-rich gas of feeding and air in burning chamber, emits a large amount of heat, and the heat major part has passed to reformation chamber and two vaporization chambers by heat-conducting plate; Stock liquid is introduced into two gasification chambers that enter hydrogen-manufacturing reactor after the snakelike heat exchange coil preheating in the left end end socket, enters the reformation chamber after the gasification, and is finally reformed in the reformation chamber and make satisfactory hydrogen mixed gas.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor is provided with gas distributor and thermocouple in its described burning chamber, and burning gas flows by gas distributor after entering burning chamber, and the position of gas distributor is parallel with the position of thermocouple in the burning chamber.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, its described gas distributor is in burning chamber, press the fluidic flow direction, be in the gas distributor in the chamber of the upstream of flowing, outlet distribution density on unit length is bigger, and for the gas distributor in the chamber that is in flow downstream, the outlet distribution density on unit length is less.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, its described burning chamber uses different catalyzer respectively with the reformation chamber, and catalyzer can also can be the wall carried catalyst with particles filled.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, the left end socket of the left end socket of burning chamber side and reformation chamber and gasification chamber side is detachable end socket, so that change combustioncatalysts and reforming catalyst.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, earlier through feed distributor, it is more even to distribute when making raw material enter gasification chamber before stock liquid enters gasification chamber for it.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, the inner panel fin structure of its burning chamber, reformation chamber and gasification chamber adopts the porous plate fin structure, and raw material is the energy thorough mixing in the chamber, and it is more even to distribute, and has overcome the defective of shell and tube reactor.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, its described snakelike heat exchange coil, its import and export are located on the outer side wall, and outlet has pipeline to communicate with the import of gasification chamber; Raw material is earlier by entering gasification chamber after the coil pipe preheating, and raw material has also reduced the temperature in the burning chamber left end end socket in preheating; Reactor self can be realized the self-heating operation simultaneously.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, it is between burning chamber and the reformation chamber, between burning chamber and the gasification chamber, and logistics mobile is cross-flow.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, after its system was stable, the combustion gases that enter burning chamber had and come from the part reformed gas that the reformation chamber self is produced; During with the supporting use of fuel cell, the combustion gases that enter burning chamber can be from anode of fuel cell tail gas, to realize the self-heating operation.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, the import and export of having nothing in common with each other in its burning chamber, gasification chamber and reformation chamber.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, its described heat-conducting plate, its thickness are 0.3～0.5mm.
Described microchannel plate-fin steam reforming hydrogen manufacturing reactor, it can be used for vehicle-mounted onboard hydrogen source system, small stationary source hydrogen generating system, and be convenient to the expansion scale.
Microchannel plate-fin steam reforming hydrogen manufacturing reactor is a kind of new hydrogen production reactor of developing on the insufficient basis of the plate type hydrogen-manufacturing reactor that has overcome existing drum type brake fixed bed hydrogen-manufacturing reactor, shell and tube hydrogen-manufacturing reactor and slab construction, is a kind of reforming hydrogen-preparation reactor that is particularly suitable on a small scale fixing hydrogen source and vehicle-mounted onboard hydrogen source system.
Relate to the coupling of strong exothermal reaction and strong endothermic reaction and strong exothermal reaction and evaporation in the plate-fin steam reforming hydrogen manufacturing reactor of microchannel, wherein the system arrangement of heat will directly have influence on the performance of reaction.In case the irrational distribution of heat in whole reaction system will cause multiple negative impact,, catalyst deactivation low as reaction conversion ratio and byproduct of reaction are many etc., and even more serious is the pipeline that this situation may be damaged reactor and link to each other with reactor.Most typical in the irrational negative impact of heat distribution is exactly the bad control of temperature of reactor, makes selectivity of catalyst and productive rate all lower.The characteristic that reactor of the present invention has made full use of uniformity of temperature profile in higher heat transfer efficiency of microchannel plate fin structure and the reactor has realized the reasonable distribution of system thermal and the steady running of system effectively.
In addition, microchannel plate-fin steam reforming hydrogen manufacturing reactor is owing to all adopted the microchannel plate fin structure in each reaction chamber, and its heat-transfer effect will be much better than the board-like reforming hydrogen-preparation reactor of slab construction; In addition, this microchannel plate-fin steam reforming hydrogen manufacturing reactor can obtain more massive reaction unit by size that increases the chamber, unit or the quantity that increases the chamber, and this has just overcome the limitation of concentric-ring pattern reactor expansion scale.Be particularly suitable on a small scale the fixedly needs of hydrogen source and removable hydrogen source.
In the reformation chamber, the reaction that takes place according to different hydrogen manufacturing mode (steam reformation, partial oxidation are reformed and complete self-heating recapitalization) also has nothing in common with each other.
In chemical process, adopt the method for steam reforming hydrogen manufacturing usually:
In this reaction process, the raw material that adds the reformation chamber can be: hydrocarbons such as alcohols such as Sweet natural gas, methyl alcohol and gasoline, they are converted into hydrogen mixed gas (comprising: hydrogen, carbon monoxide, carbonic acid gas etc.) under the effect of reforming catalyst.The very suitable long stable operation of steam reforming hydrogen manufacturing, and the concentration of hydrogen is higher in the reformed gas, steam reformation is a strong endothermic reaction, the quality of heat transfer directly affects speed, transformation efficiency and the selectivity of reaction.
The partial oxidation reformation hydrogen production is exactly to add a certain amount of oxygen (or air) in the unstripped gas system, makes part methyl alcohol and oxygen generation combustion reactions, and a large amount of heats of emitting are used to provide methanolysis.
Its reactional equation is as follows:
Self-heating reforming hydrogen manufacturing is steam reformation and partial oxidation combination of them, and its reactional equation is as follows:
In the reaction process, the heat that the partial oxidation reformation produces is utilized by steam reformation fully, thereby makes that the relative partial oxidation of temperature (about 500 ℃) of whole reaction system is low.Certainly in order to make the better effects if of reformation, a kind of catalyzer of excellent property is essential.
Because microchannel plate fin structure heat transfer efficiency height, in the present invention, the method for hydrogen manufacturing adopts steam reforming hydrogen manufacturing.In concrete invention is implemented, can obtain containing the reformed gas of higher hydrogen concentration, and the reforming reaction temperature is lower, reacts stable, easy to operate.
Compare with United States Patent (USP) (patent No. US 6,190,624 B1), the filling method of catalyzer is simple among the present invention.In the present invention, all relate to chemical reaction in heat-absorbing chamber and the heat release chamber, and never mix between the fluid of heat absorption and heat release.In addition, in order to resolve the heat coupled problem between the heat absorption of catalyst combustion reaction heat release and steam reformation better, the microchannel plate-fin steam reforming hydrogen manufacturing reactor of the present invention's design has made full use of the high characteristics of microchannel plate fin structure heat transfer efficiency, all adopt the structure of porous plate wing in the inside in reformation, gasification and each chamber of catalyticcombustion, the aperture that gathers on the fin constantly breaks the thermal resistance frictional belt, thereby has improved heat transfer property.In addition, the porous structure makes that fluid distributes in each chamber more even, and the heat exchange effect is better; Its volume is less relatively simultaneously; Be convenient to the expansion scale; Integrated, the equipment integration of technology can integrate preheating vaporization, reformation, combustion reactions; The inside reactor Btu utilization is reasonable, has realized heat coupling preferably between thermopositive reaction and thermo-negative reaction, vaporization and the reaction.
Description of drawings
Fig. 1 is a vertical view of microchannel plate-fin steam reforming hydrogen manufacturing reactor profile;
Fig. 2 is a sectional side view of microchannel plate-fin steam reforming hydrogen manufacturing reactor profile;
Fig. 3 is a sectional side view of microchannel plate-fin steam reforming hydrogen manufacturing reactor profile;
Fig. 4 is the porous plate fin structure figure in the plate-fin steam reforming hydrogen manufacturing reactor lumen of microchannel;
Fig. 5 is the serpentine heat exchanger structure diagram of burning chamber afterbody in the plate-fin steam reforming hydrogen manufacturing reactor of microchannel;
Fig. 6 is the circular gas distributor in the plate-fin steam reforming hydrogen manufacturing reactor lumen of microchannel;
Fig. 7 is the square gas distributor in the plate-fin steam reforming hydrogen manufacturing reactor lumen of microchannel;
Fig. 8 is the schema in the concrete embodiment of microchannel plate-fin steam reforming hydrogen manufacturing reactor;
Fig. 9 is the change curve of reformation cavity temperature before and after burning gas is switched in the experiment;
Figure 10 is a burning chamber variation of temperature graphic representation before and after burning gas is switched in the experiment;
Figure 11 is the interior temperature profile of the gasification chamber of microchannel plate-fin steam reforming hydrogen manufacturing reactor;
Figure 12 is the reformation cavity temperature distribution plan of microchannel plate-fin steam reforming hydrogen manufacturing reactor;
Figure 13 is the interior temperature profile of the burning chamber of microchannel plate-fin steam reforming hydrogen manufacturing reactor;
Table 1 is the experimental result of steam reformation of methanol to produce hydrogen in the plate-fin steam reforming hydrogen manufacturing reactor of microchannel.
Embodiment
As Fig. 1, Fig. 2 and microchannel plate-fin steam reforming hydrogen manufacturing reactor shown in Figure 3, design power is 0.5KW.Microchannel plate-fin steam reforming hydrogen manufacturing reactor, main part is the microchannel plate fin structure, adds several end sockets and is welded, one has five chambeies forms, 25, one reformation chambeies 24 of two burning chambers and two gasification chambers 23 are arranged, all have the thick heat-conducting plate of 0.4mm 30 to be separated by between chamber and the chamber.Reformation chamber 24 of two burning chamber 25 therebetween, the opposite side of two burning chambers respectively has a gasification chamber 23, catalyst combustion reaction takes place in hydrogen-rich gas and air in burning chamber 25, emit a large amount of heat, this part heat major part has passed to reformation chamber 24 and two vaporization chambers 23 by the heat-conducting plate 30 of 0.4mm.Stock liquid is introduced into two gasification chambers 23 of microchannel plate-fin steam reforming hydrogen manufacturing reactor, enters reformation chamber 24 after the gasification, and is finally made satisfactory hydrogen mixed gas by reformation in reformation chamber 24.
The burning chamber 25 of reactor, gasification chamber 23 link to each other with two imports 11,12 respectively, and burning chamber 25 the other ends, reformation chamber 24 link to each other with two outlets 32,13 respectively.
Still reform chamber 24 and gasification chamber 23 of burning chamber 25 no matter, the inner panel fin structure in its chamber all adopts porous plate fin structure (see figure 4).
Burning gas enters burning chamber 25 and has passed through a gas distributor 29, its position is parallel with the position of thermocouple 28 in the burning chamber 25, gas distributor 29 can adopt two kinds of different structures, a kind of circular gas distributor (Fig. 6), a kind of square gas distributor (Fig. 7).
Combustion tail gas gathering owing to a large amount of hot gas flows in the outlet of burning chamber 25 afterbodys makes temperature higher relatively, (position shown in the ε among Fig. 1, Fig. 3) added a snakelike heat exchange coil (see figure 5) in burning chamber 25 left side end sockets 33, raw material flows out from 15 after can entering this coil pipe preheating by 14 among Fig. 1 earlier, enter gasification chamber 23 by adding pipeline then, raw material has also reduced the temperature in the burning chamber 25 afterbodys outlet end socket in preheating.
The import and export of having nothing in common with each other in burning chamber 25 and reformation chamber 24.
Burning chamber 25 uses different catalyzer respectively with reformation chamber 23, and catalyzer can also can be the wall carried catalyst with particles filled.
End at burning chamber 25 is detachable end socket 33, is convenient to change combustioncatalysts like this; An end of chamber 24 and gasification chamber 23 reform simultaneously also for detachable end socket 27, be convenient to change reforming catalyst.
Earlier through a feed distributor 26, it is more even to distribute when it can make raw material enter gasification chamber 23 before stock liquid enters gasification chamber 23.
Microchannel plate-fin steam reforming hydrogen manufacturing reactor can obtain more massive reaction unit by size that increases the chamber, unit or the quantity that increases the chamber, and this has just overcome the limitation of concentric-ring pattern reactor expansion scale.In order to overcome the uneven situation of traditional drum type brake fixed-bed reactor temperature distribution, utilized gas distributor 29 (Fig. 6, Fig. 7) in the plate-fin reactor, make that the unstripped gas at each position distributes more even in reaction chamber, and employing porous plate-fin structure, fluid can also mix in reaction chamber fully, the raising of heat transfer efficiency simultaneously also makes structure of reactor more compact, and volume is less, has avoided owing to the radially long temperature distributing disproportionation that brings.Simultaneously, for the heat transmission resistance that reduces to reform between heat absorption and the burning heat release, improve heat-transfer effect, improve reaction efficiency and improve reaction preference, microchannel of the present invention plate-fin steam reforming hydrogen manufacturing reactor has made full use of the high characteristics of microchannel plate fin structure heat transfer efficiency, burning chamber 25, gasification chamber 23 and reformation chamber 24 are all designed in same plate fin structure, and the fluid flow direction in two simultaneously adjacent chambeies is cross-flow passes.Combustion gases enter the burning chamber 25 that combustioncatalysts is housed from import 11, are flowed out by outlet 32 by gas distributor 29; Stock liquid is earlier by being arranged on the serpentine heat exchanger heat exchange of burning chamber 25 afterbodys, then by import 12 process feed distributors 26, enter gasification chamber 23, enter the reformation chamber 24 that reforming catalyst is housed after stock liquid is gasified fully in gasification chamber 23 again, in reformation chamber 24, raw material makes the reformed gas that contains a large amount of hydrogen through steam reformation, and derives reactor by outlet 13.Stream in stock liquid, unstripped gas and the burning chamber 25 is cross-flow passes.
The liquid starting material that adopts can be selected hydrocarbons such as alcohols such as Sweet natural gas, methyl alcohol and gasoline.In order to be briefly described the certain situation in the actual implementation process, now selecting the first alcohol and water is that raw material illustrates, and chemical reaction mainly carries out in burning chamber 25 and reformation chamber 24, and wherein combustion reactions is mainly carried out in two combustion zones:
Two districts mainly are the waste gas that makes full use of fuel cell in order to simulate, and it mainly acts on two: one, the vaporization for material provides heat; Two, the reforming reaction for reformation chamber 24 provides enough energy.Steam reforming reaction is mainly carried out in reformation chamber 24:
Microchannel plate-fin steam reforming hydrogen manufacturing reactor experiment flow is in the specific implementation seen Fig. 8.In the experiment; feed shielding gas (being generally nitrogen) by the gasification chamber 23 and the reformation chamber 24 of mass flowmeter 61 in microchannel plate-fin steam reforming hydrogen manufacturing reactor 69 earlier; the pipeline that left-hand broken line is represented among the figure is controlled with mass flowmeter 61; burning chamber 25 bubbling airs and hydrogen in microchannel plate-fin steam reforming hydrogen manufacturing reactor 69 by a certain percentage; when reformation chamber 24 reaches certain temperature; then close protection gas; begin to send methanol aqueous solution to through the gasification chamber 23 and the reformation chamber 24 of external heat exchanger 63 in microchannel plate-fin steam reforming hydrogen manufacturing reactor 69 earlier with constant-flux pump 62; produce reformed gas, reformed gas is by external water cooler 64; gas-liquid separator 65; on-line analysis is carried out by gas-chromatography in moisture eliminator 66 backs.When reforming reaction is stablized, just can end the hydrogen of left side pipeline, return burning chamber 25 and carry out catalyst combustion reaction, reach complete self-heating operation and use from the reformation chamber the 24 part reformed gases that produce instead.Result of experiment shows that in the handoff procedure of burning gas, the temperature of reaction fluctuation is (seeing Fig. 9,10) not quite, and the arrow indication is the burning gas switching point among the figure.Temperature in the experiment, stratographic sampling are by computer workstation 67 controls.When reforming reactor and fuel cell joint-trial, the gas that returns burning chamber 25 is mainly from the anode exhaust gas of fuel cell.In addition, the tensimeter 68 from schema can know that the pressure drop of whole reactor is under normal circumstances all very little, can ignore.
The microchannel plate-fin steam reforming hydrogen manufacturing reactor of a 0.5KW power that manufactures and designs by above-mentioned design, its volume is 100 * 80 * 38mm
3Producible hydrogen gas mixture scale: 0.45m in the experiment
3/ h, density of hydrogen is greater than 74% in the reformed gas, and CO concentration is less than 1.5%, and producing the hydrogen rate is 2.0m
3H
2/ Kg CH
3About OH, system pressure is 0.00～0.15MPa, can be according to demand in the practical application, and pressure-controlling is at 0～3MPa.Concrete experimental data sees Table 1.In order to grasp the characteristic of microchannel plate-fin steam reforming hydrogen manufacturing reactor better, in the experiment detailed measurements temperature distribution of gasification chamber 23, reformation chamber 24 and burning chamber 25 in the plate-fin steam reforming hydrogen manufacturing reactor of microchannel, the particular location of thermocouple 28 as shown in Figure 1 in the plate-fin steam reforming hydrogen manufacturing reactor of microchannel, three thermocouples 28 are set in the burning chamber 25 altogether, spacing between the thermocouple 28 is shown in C1, C2 and C3, and its temperature that records is expressed as burning 1, burning 2 respectively and burns 3 in temperature profile; Three thermocouples 28 are set in the reformation chamber 24 altogether, spacing between the thermocouple 28 is shown in R1, R2 and R3, three thermocouples 28 are set in the gasification chamber 23 altogether, spacing between the thermocouple 28 is also shown in R1, R2 and R3, these thermocouples 28 all can be along the axial direction due translation of reactant flow, these thermocouple 28 measured temperature in temperature profile, be expressed as respectively and reform 1, reform 2 and reform 3 and gasify 1, gasification 2 and gasify 3; The concrete data of temperature distribution are seen Figure 11,12,13.In Figure 11, can see, reaction raw materials is after process is arranged on the sinuous coil preheating of burning chamber 25 afterbodys, and temperature is very high, after entering gasification chamber 23, the temperature of raw material can remain on more than 200 ℃ basically, and more even in gasification chamber 23 interior temperature distribution.It among Figure 12 the temperature distribution history in reformation chamber 24 in the experiment, reformation chamber 24 each point temperature distribute more even in experimentation, the temperature of reforming reaction is controlled at about 240 ℃, 24 exits, reformation chamber are subjected to external environment influence big slightly, chamber 24 is inner low so the temperature in exit is reformed, its reason mainly is that present system is less, if when device is big slightly, this phenomenon will reduce greatly.Burning chamber 25 temperature keep also relatively more consistently among Figure 13 at burning chamber 25 middle parts.Microchannel of the present invention plate-fin steam reforming hydrogen manufacturing reactor can reach the design requirements of 0.5KW.
The present invention is specially adapted to (1～1000NM on a small scale
3/ hr) the fixing hydrogen production reaction of hydrogen source and portable hydrogen source.
Claims (13)
1, a kind of microchannel plate-fin steam reforming hydrogen manufacturing reactor, main part is the microchannel plate fin structure, adds several end sockets and is welded, it is characterized in that, two burning chambers are arranged, and a reformation chamber and two gasification chambers are formed, and all have heat-conducting plate to be separated by between chamber and the chamber; Reformation chamber of two burning chamber therebetween, respectively there is a gasification chamber in the outside of two burning chambers; Respectively there is an end socket at the two ends of two burning chambers, and right-hand member end socket right side is provided with inlet mouth, and left end is a detachable end socket, vertically are provided with the air outlet on its lower wall, are provided with snakelike heat exchange coil in the left end end socket; Also respectively there is an end socket at the two ends of reformation chamber and two gasification chambers, the left end of reformation chamber and two gasification chambers communicates through left end socket, right-hand member is after dividing plate is isolated, the right-hand member of two gasification chambers communicates with right end socket by feed distributor, and communicate with the inlet mouth on the right wall of right end socket, the right-hand member in reformation chamber communicates by the air outlet on the right wall of pipeline and right end socket; During work, catalyst combustion reaction takes place in the hydrogen-rich gas of feeding and air in burning chamber, emits a large amount of heat, and the heat major part has passed to reformation chamber and two vaporization chambers by heat-conducting plate; Stock liquid is introduced into two gasification chambers that enter hydrogen-manufacturing reactor after the snakelike heat exchange coil preheating in the left end end socket, enters the reformation chamber after the gasification, and is finally reformed in the reformation chamber and make satisfactory hydrogen mixed gas.
2, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor, it is characterized in that, be provided with gas distributor and thermocouple in the described burning chamber, burning gas flows by gas distributor after entering burning chamber, and the position of gas distributor is parallel with the position of thermocouple in the burning chamber.
3, microchannel as claimed in claim 2 plate-fin steam reforming hydrogen manufacturing reactor, it is characterized in that, described gas distributor is in burning chamber, press the fluidic flow direction, be in the gas distributor in the chamber of the upstream of flowing, outlet distribution density on unit length is bigger, and for the gas distributor in the chamber that is in flow downstream, the outlet distribution density on unit length is less.
4, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that described burning chamber uses different catalyzer respectively with the reformation chamber, and catalyzer can also can be the wall carried catalyst with particles filled.
5, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that the left end socket of the left end socket of burning chamber side and reformation chamber and gasification chamber side is detachable end socket, so that change combustioncatalysts and reforming catalyst.
6, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that, earlier through feed distributor, it is more even to distribute when making raw material enter gasification chamber before stock liquid enters gasification chamber.
7, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor, it is characterized in that the inner panel fin structure of burning chamber, reformation chamber and gasification chamber adopts the porous plate fin structure, raw material is the energy thorough mixing in the chamber, it is more even to distribute, and has overcome the defective of shell and tube reactor.
8, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that, described snakelike heat exchange coil, and its import and export are located on the outer side wall, and outlet has pipeline to communicate with the import of gasification chamber; Raw material is earlier by entering gasification chamber after the coil pipe preheating, and raw material has also reduced the temperature in the burning chamber left end end socket in preheating; Reactor self can be realized the self-heating operation simultaneously.
9, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that, between burning chamber and the reformation chamber, between burning chamber and the gasification chamber, logistics mobile is cross-flow.
10, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that, after system was stable, the combustion gases that enter burning chamber had and come from the part reformed gas that the reformation chamber self is produced; During with the supporting use of fuel cell, the combustion gases that enter burning chamber can be from anode of fuel cell tail gas, to realize the self-heating operation.
11, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that the import and export of having nothing in common with each other in burning chamber, gasification chamber and reformation chamber.
12. microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that described heat-conducting plate, its thickness are 0.3～0.5mm.
13, microchannel as claimed in claim 1 plate-fin steam reforming hydrogen manufacturing reactor is characterized in that, can be used for vehicle-mounted onboard hydrogen source system, small stationary source hydrogen generating system, and be convenient to the expansion scale.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101223441A CN1284721C (en) | 2003-12-16 | 2003-12-16 | Microchannel plate-fin type water vapour reforming reactor for hydrogen production |
Applications Claiming Priority (1)
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| CN100441496C (en) * | 2006-10-16 | 2008-12-10 | 华南理工大学 | Plate type hydrogen-manufacturing reactor with oxygen spray structure |
| CN100450916C (en) * | 2006-04-10 | 2009-01-14 | 中国科学院大连化学物理研究所 | Mini reforming hydrogen-preparation reactor |
| CN100535572C (en) * | 2005-12-28 | 2009-09-02 | 中国科学院大连化学物理研究所 | Catalytic combustion evaporator |
| CN101307994B (en) * | 2008-07-03 | 2010-06-02 | 上海交通大学 | Metal hydrides plate-fin heat exchanger |
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| CN102447122A (en) * | 2010-10-13 | 2012-05-09 | 中国科学院大连化学物理研究所 | Integrated catalytic combustion evaporator |
| CN102452642A (en) * | 2010-10-27 | 2012-05-16 | 中国科学院大连化学物理研究所 | Compact natural gas reforming hydrogen producing reactor |
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| CN103192190A (en) * | 2013-04-15 | 2013-07-10 | 青岛兰石重型机械设备有限公司 | Welding method for middle shell cover, with reinforcing ring, of reforming reactor |
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| CN102452642B (en) * | 2010-10-27 | 2013-08-21 | 中国科学院大连化学物理研究所 | Compact natural gas reforming hydrogen producing reactor |
| CN102502494A (en) * | 2011-11-04 | 2012-06-20 | 中国人民解放军防化指挥工程学院 | Laminated type reactor for hydrogen production by reforming alcohols |
| CN102502494B (en) * | 2011-11-04 | 2013-04-24 | 中国人民解放军防化指挥工程学院 | Laminated type reactor for hydrogen production by reforming alcohols |
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| CN109956449A (en) * | 2017-12-14 | 2019-07-02 | 中国科学院大连化学物理研究所 | A kind of parallel type methanol-water reforming hydrogen-preparation reactor |
| 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 |
| CN109289713A (en) * | 2018-10-18 | 2019-02-01 | 辽宁石油化工大学 | A kind of mosquito-repellent incense coil pipe isothermal reactor and application method |
| CN109289713B (en) * | 2018-10-18 | 2021-04-20 | 辽宁石油化工大学 | Mosquito-repellent incense coil isothermal reactor and using method thereof |
| CN109911849A (en) * | 2019-03-29 | 2019-06-21 | 摩氢科技有限公司 | Self-heat-supply reforming reaction device and hydrogen making machine suitable for hydrogen making machine |
| CN110386589A (en) * | 2019-08-06 | 2019-10-29 | 强伟氢能科技有限公司 | A kind of high throughput methanol-water reformation hydrogen production micro passage reaction |
| CN112993315A (en) * | 2019-12-14 | 2021-06-18 | 中国科学院大连化学物理研究所 | Heat coupling methanol reforming hydrogen production fuel cell system |
| CN111333028A (en) * | 2020-04-28 | 2020-06-26 | 上海博氢新能源科技有限公司 | Multi-return-stroke reforming hydrogen production reactor |
| CN112960647A (en) * | 2021-03-16 | 2021-06-15 | 哈尔滨工业大学 | Reforming hydrogen production and catalytic combustion integrated device with variable catalyst particle arrangement |
| CN115504433A (en) * | 2022-09-30 | 2022-12-23 | 大连大学 | Combustion coupling electric heating device for integrated methanol reforming hydrogen production reactor |
| CN115504433B (en) * | 2022-09-30 | 2023-12-08 | 大连大学 | Combustion coupling electric heating device for integrated methanol reforming hydrogen production reactor |
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