CN201762094U - Distributed natural gas hydrogen-making reactor - Google Patents
Distributed natural gas hydrogen-making reactor Download PDFInfo
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- CN201762094U CN201762094U CN2010202999258U CN201020299925U CN201762094U CN 201762094 U CN201762094 U CN 201762094U CN 2010202999258 U CN2010202999258 U CN 2010202999258U CN 201020299925 U CN201020299925 U CN 201020299925U CN 201762094 U CN201762094 U CN 201762094U
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Abstract
The utility model discloses to a distributed natural gas hydrogen-making reactor, which comprises a two-way reflux annular gas inlet passage formed by a gas inlet passage outer wall thin plate and a gas inlet passage inlet wall thin plate and a two-way reflux annular gas exhaust passage formed by a gas exhaust passage outer wall thin plate and a gas exhaust passage inner wall thin plate, and is characterized in that an annular stripped belt-shaped gas inlet passage spacer thin plate is inserted in the gas inlet passage to divide the gas inlet passage into a first gas flow passage and a second gas flow passage. By adopting the reactor, fuel gas and oxidizing gas which participate into the reaction can enter the center of the reactor in a non-premixed state, so as to avoid the problem of flame drift resulted from premixing before the fuel gas and the oxidizing gas enter porous medium and avoid the explosion hazard due to premixing, so that the reactor can be widely applied to combustion reaction devices of low-concentration combustible gas including drafty gas, natural gas, biogas, oil reservoir gas in petroleum production, or combustible waste gas in chemical engineering production.
Description
Technical field
The utility model belongs to hydrogen producer, particularly a kind of distributed natural gas hydrogen production reactor.
Background technology
Hydrogen Energy as a kind of cleaning, efficient, safety, the continuable energy, is regarded as the most potential clean energy in this century, also be regarded as solving the Greenhouse effect problem, improve capacity usage ratio effectively substitute secondary energy.The source of hydrogen is more extensive, all contains a large amount of hydrogen in fossil oil, plant and the organic waste, but the pure hydrogen that occurring in nature can directly utilize is considerably less, can only prepare from other energy by specific method.90% hydrogen is all produced by gas water steam reforming reaction or partial oxidation in the world at present.
The extensive hydrogen manufacturing of traditional Sweet natural gas, because facility investment is huge, technical renovation slowly relatively always; On the other hand, because the storage of hydrogen and transportation are relatively more difficult, and along with the continuous development of distributed natural gas hydrogen production technical need in recent years, the research and development of the technology of distributed small-scale hydrogen manufacturing have obtained increasing support and attention.
The Chinese utility application of application number 200710020394.7 has proposed " a kind of combustion unit of low concentration gaseous hydrocarbon ", be to surround ring-type induction trunk and exhaust-duct by lamellar outside wall surface and inner-wall surface, form the gas channel of bidirectional adverse current, be communicated with the combustion chamber that is positioned at annular channel circle center; The combustion chamber is built-in with porous material, and porous material is provided with an electric heating element.The reaction compartment of this combustion unit is in the porous material zone, make the heat exchange mode of conventional poor efficiency based on gas radiation and convection current change the high efficient heat exchanging based on the radiation of high-temp solid medium into, its rate of combustion height, flameholding, pollutant emission is low, the burner volume is little, compact construction, load regulation range are wide.The induction trunk and the exhaust-duct of bidirectional adverse current heat exchange used in the outside of combustion unit, make low concentration gaseous hydrocarbon before arriving central combustion chamber, can rise to higher temperature, the thermal insulation of oppose side wall simultaneously requires low, has improved efficiency of combustion, has reduced Financial cost.But, because what enter reactor from induction trunk is the mixture of fuel and oxygenant, after in a single day the size of reactor is determined, when if fuel in the air inlet composition and oxidant ratio change, perhaps the type of refuelling the time, air inlet may just reach point of ignition in no show central combustion chamber, also might after having flow through central combustion chamber, just have and to reach point of ignition, feasible reaction can not be stabilized in the porous material in the central combustion chamber to be carried out, even it is flame-out, make porous material at stable burning flame, improve efficiency of combustion, expand the poor combustion limit etc. significantly superiority can't be embodied, also just be difficult to reach this Design of device purpose, and, the rapid reaction in induction trunk or exhaust-duct of the pre-mixed gas of pyritous methane and air, device has explosion hazard.
The Chinese utility application of application number 200810184969.3 has proposed " a kind of natural gas hydrogen production plant and method ", described device is made up of reverse heat exchanger, the reaction coil pipe that places the porous medium at reverse heat exchanger center and run through the reverse heat exchanger heat exchanger channels, the feeding stoichiometric ratio is 1 premixed fuel gas in reverse heat exchanger, and the porous medium zonal combustion of the heart therein forms hot environment; In the reaction coil pipe, feed pure natural gas again, this strand Sweet natural gas by with reverse heat exchanger, the heat exchange of high temperature porous medium after, reach cracking temperature, reaction generates charcoal and hydrogen.Though this device can produce pure hydrogen, be not to be to continue to produce hydrogen storage equipment, after operation for some time, the charcoal that reaction generates accumulates in reaction coil pipe inside, needs to feed steam and comes carbon deposit.On the one hand, carbon deposit and steam reaction generate carbon monoxide and hydrogen, are not to be pure hydrogen, if be purpose to obtain pure hydrogen, device needs to switch operating mode, can't continuous service; On the other hand, the feeding of steam has reduced the temperature of reaction coil pipe, makes the natural gas pyrolysis hydrogen production reaction to continue, and needs the timed interval when restarting; Simultaneously, when the water vapour of feeding and high temperature carbon deposit react, also can make reaction tray pipe internal surface layer degrade reaction, reduce the work-ing life of device.
The utility model content
The utility model is for avoiding above-mentioned existing in prior technology weak point, a kind of distributed natural gas hydrogen production reactor is provided, with realize Sweet natural gas efficiently, safely, stablize distributed hydrogen manufacturing.
The utility model technical solution problem adopts following technical scheme:
The utility model distributed natural gas hydrogen production reactor, comprise: surround the ring-type induction trunk and the ring-type exhaust-duct of bidirectional adverse current by induction trunk outer wall thin plate and induction trunk inwall thin plate and by exhaust-duct outer wall thin plate and exhaust-duct inwall thin plate, place the porous medium in central reaction district in the multiply aheat exchanger and place priming bar in the porous medium; Its constructional feature is: insert the induction trunk separator sheet of a ring-type banding pattern in induction trunk, described induction trunk is divided into first strand of induction trunk and second strand of induction trunk.
The constructional feature of the utility model distributed natural gas hydrogen production reactor also is:
The volume in described central reaction district be whole reactor volume 10%～50%, in described central reaction district, with 1～5 dividing plate central reaction is distinguished and to be divided into " it " font baffling passage.
The number of turns of described ring-type induction trunk and ring-type exhaust-duct is 3～20, the square ring-type that is shaped as spiral circular or spirals.
The initial inflow region of air-flow of described priming bar centering reaction zone, the initial inflow region of described air-flow are second burst of air inlet exit of second strand of induction trunk.
Described porous medium is piled up by honeycombed ceramic heat storage body, ceramic heat-storing bead or foamed ceramics and is formed.
The outside surface of described porous medium is coated with catalyst layer.
Compared with the prior art, the utility model beneficial effect is embodied in:
1, the adding of induction trunk separator sheet in the utility model, can make the fuel gas that participates in reaction and oxidizing gas (as air, oxygen etc.) separately be delivered to reactor center porous medium zone with non-premixed state, can be before reactant gases enters the central reaction district because of not mixing, heat up and react in advance, and it is big by thermal conductivity and thermal capacity, the porous medium that heat storage efficiency is high, fully stable reaction is limited in the central reaction district, avoided fuel gas and oxidizing gas before entering porous medium because of the combustion flame drifting problem takes place in pre-mixing, also avoided the danger of the blast that causes therefrom.
2, the utility model is by the dividing wall type heat exchange of multiply aheat exchanger, can make the temperature of fuel gas and oxidizing gas be elevated to higher level, the point of ignition that is higher than fuel gas, the limit has reclaimed the deflated heat of high temperature again simultaneously, significantly reduced the deflated temperature levels, realize the heat oneself recycle of system, improved the temperature levels in central reaction district, helped the lifting of speed of response; In addition, the reactor outside wall temperature is lower, and heat lost by radiation is few, has also reduced the insulation requirement.Therefore, the capacity usage ratio of single unit system reaches maximization, and the reaction efficiency of fuel gas is promoted greatly.
3, the utility model compact overall structure, integrate functions such as the efficient preheating of reactant gases, pyroreaction, limit waste heat recovery, equipment oneself insulation, the integrated level height, can realize the miniaturization continuous production, equipment investment cost, working cost are low, can satisfy the requirement of distributed hydrogen manufacturing.
Description of drawings
Fig. 1 is the structural representation of the utility model embodiment 1.
Fig. 2 is the structural representation of the utility model embodiment 2.
Fig. 3 is the structural representation of the utility model embodiment 3.
Number in the figure: 1 first burst of gas inlet, 2 second bursts of gas inletes, 3 induction trunk outer wall thin plates, 4 induction trunk separator sheet, 5 induction trunk inwall thin plates, 6 first bursts of induction trunk outlets, 7 second bursts of induction trunk outlets, 8 priming bares, 9 porous mediums, 10 first strands of induction trunks, 11 second strands of induction trunks, 12 exhaust-ducts, 13 exhaust outlets, 14 exhaust-duct inwall thin plates, 15 exhaust-duct outer wall thin plates, 16 exhaust-ducts inlet, 17 central reaction districts, 18 multiply aheat exchangers, 19 dividing plates.
Embodiment
Embodiment 1:
Fig. 1 has provided multiply aheat exchanger 18 for the number of turns of spiral circle ring-type, induction trunk and exhaust-duct 12 is 3 circles, central reaction district 17 does not have the present embodiment structural representation of separating under the situation.
This distributed natural gas hydrogen production reactor, comprise: by induction trunk outer wall thin plate 3 and induction trunk inwall thin plate 5, and by exhaust-duct outer wall thin plate 15 and exhaust-duct inwall thin plate 14 surround bidirectional adverse current ring-type induction trunk and exhaust-duct 12, place the porous medium 9 in central reaction districts 17 in the multiply aheat exchanger 18 and and place priming bar 8 in the porous medium 9.
In concrete the enforcement, the number of turns of ring-type induction trunk and ring-type exhaust-duct 12 can be for 3～20 roads, be shaped as the circular or square ring-type for spiraling of spiraling.In induction trunk, insert a ring-type banding pattern induction trunk separator sheet 4, induction trunk is divided into first strand of induction trunk 10 and second strand of induction trunk 11.Flow to first strand of identical induction trunk 10, second strand of induction trunk 11 and flow to different exhaust-duct 12 and constituted multiply aheat exchanger 18.
The volume in central reaction district 17 is 10%～50% of a whole reactor, and wherein the porous medium 9 of Bu Zhiing is big by thermal conductivity and thermal capacity, and the honeycombed ceramic heat storage body that heat storage efficiency is high, ceramic heat-storing bead or foamed ceramics are piled up and formed.The outside surface of porous medium 9 can catalyst layer, and catalyzer can use one or more among Co-Mo, Ni, Rh or the Pt.
The initial inflow region of air-flow of priming bar 8 centering reaction zones 17, the initial inflow region of air-flow is the mixing region that crosses that two bursts of air inlets enter central reaction district 17, the second strand of induction trunk that is second strand of induction trunk 11 exports near the gas flowfield downstream of 7 (also can be first burst of induction trunk outlet 6), is used for the ignition trigger of reactor.
During operation, at first feed stoichiometric ratio respectively and be 1 Sweet natural gas and air (or oxygen rich gas) from first burst of gas inlet 1 and second burst of gas inlet 2, start-up point lighted torch 8, Sweet natural gas is caught fire in the porous medium 9 in central reaction district 17, combustion reactions, the temperature of porous medium 9 raises rapidly, the products of combustion that produces is discharged by exhaust outlet 13 behind exhaust-duct inlet 16 and exhaust-duct 12, in the outflow process with first strand of induction trunk 10 and second strand of induction trunk 11 in Sweet natural gas and air (or oxygen rich gas) the dividing wall type heat exchange takes place, in reduction self temperature, make the temperature levels of Sweet natural gas and air (or oxygen rich gas) significantly rise, thereby further promoted the temperature of reaction in central reaction district 17.
When the temperature of center reaction zone 17 is higher than more than 800 ℃, calculate to regulate change the air inlet ratio of Sweet natural gas and air in first strand of induction trunk 10 and the second strand of induction trunk 11 according to actual design, the appropriate chemical equivalence ratio scope of natural gas hydrogen preparation is 2.0～3.0 under the general situation, make Sweet natural gas and air in porous medium 9, hydrogen production reaction take place, generate carbon monoxide and hydrogen.
This reactor also can be used for comprising the combustion reaction device of the low-concentration combustible gas of the combustible exhaust gas that discharges in the oil reservoir gas of coal mine to ventilate mash gas gas, Sweet natural gas, biogas, oil production or the Chemical Manufacture.
Embodiment 2:
Fig. 2 has provided multiply aheat exchanger 18 for the number of turns of spiral circle ring-type, induction trunk and exhaust-duct 12 is three roads, central reaction district 17 is furnished with two example structure synoptic diagram under dividing plate 19 situations.
In the present embodiment, two dividing plates 19 that increase in the central reaction district 17 are separated into " it " font baffling passage with central reaction district 17.All the other constitutional featuress are identical with embodiment 1, and the operation method is also identical with embodiment 1.
Embodiment 3:
Fig. 3 has provided multiply aheat exchanger 18 for the number of turns of square ring-type, induction trunk and the exhaust-duct 12 of spiraling is three roads, central reaction district 17 is furnished with two example structure synoptic diagram under dividing plate 19 situations.
Other structure formation in the present embodiment is identical with embodiment 2, and the operation method is identical with embodiment 1.
Claims (6)
1. distributed natural gas hydrogen production reactor, comprise: surround ring-type induction trunk and ring-type exhaust-duct (12) of bidirectional adverse current by induction trunk outer wall thin plate (3) and induction trunk inwall thin plate (5) and by exhaust-duct outer wall thin plate (15) and exhaust-duct inwall thin plate (14), place the porous medium (9) in multiply aheat exchanger (18) interior central reaction district (17) and place priming bar (8) in the porous medium (9); It is characterized in that: in induction trunk, insert the induction trunk separator sheet (4) of a ring-type band, described induction trunk is divided into first strand of induction trunk (10) and second strand of induction trunk (11).
2. distributed natural gas hydrogen production reactor according to claim 1, the volume that it is characterized in that described central reaction district (17) be whole reactor volume 10%～50%, in described central reaction district (17), central reaction district (17) are separated into " it " font baffling passage with 1～5 dividing plate (19).
3. distributed natural gas hydrogen production reactor according to claim 1 is characterized in that the number of turns of described ring-type induction trunk and ring-type exhaust-duct (12) is 3～20, the square ring-type that is shaped as spiral circular or spirals.
4. distributed natural gas hydrogen production reactor according to claim 1, the initial inflow region of air-flow that it is characterized in that described priming bar (8) centering reaction zone (17), the initial inflow region of described air-flow are that second burst of air inlet outlet (7) of second strand of induction trunk (11) located.
5. distributed natural gas hydrogen production reactor according to claim 1 is characterized in that described porous medium (9) is formed by honeycombed ceramic heat storage body, ceramic heat-storing bead or foamed ceramics accumulation.
6. distributed natural gas hydrogen production reactor according to claim 1 is characterized in that the outside surface of described porous medium (9) is coated with catalyst layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202999258U CN201762094U (en) | 2010-08-16 | 2010-08-16 | Distributed natural gas hydrogen-making reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202999258U CN201762094U (en) | 2010-08-16 | 2010-08-16 | Distributed natural gas hydrogen-making reactor |
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| Publication Number | Publication Date |
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| CN201762094U true CN201762094U (en) | 2011-03-16 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2010202999258U Expired - Lifetime CN201762094U (en) | 2010-08-16 | 2010-08-16 | Distributed natural gas hydrogen-making reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101913560A (en) * | 2010-08-16 | 2010-12-15 | 合肥工业大学 | Distributed natural gas hydrogen production reactor |
-
2010
- 2010-08-16 CN CN2010202999258U patent/CN201762094U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101913560A (en) * | 2010-08-16 | 2010-12-15 | 合肥工业大学 | Distributed natural gas hydrogen production reactor |
| CN101913560B (en) * | 2010-08-16 | 2012-07-25 | 合肥工业大学 | Distributed natural gas hydrogen production reactor |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20110316 Effective date of abandoning: 20120725 |