CN202089764U - Portable ethanol self-heating hydrogen production reactor - Google Patents
Portable ethanol self-heating hydrogen production reactor Download PDFInfo
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- CN202089764U CN202089764U CN201120147490XU CN201120147490U CN202089764U CN 202089764 U CN202089764 U CN 202089764U CN 201120147490X U CN201120147490X U CN 201120147490XU CN 201120147490 U CN201120147490 U CN 201120147490U CN 202089764 U CN202089764 U CN 202089764U
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- foam layer
- ceramic foam
- reacting cylinder
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Abstract
The utility model discloses a portable ethanol self-heating hydrogen production reactor, which comprises a reaction cylinder body, two pairs of inner and outer flange covers, an inlet tube and an outlet tube, a distributor and a ceramic foam layer carrying a catalyst. The inner flange covers are welded at both the upper end and the lower end of the reaction cylinder body, the inner and outer flange covers are sealed in butt joint mode, the inlet tube and the outlet tube are respectively welded on the outer sides of the outer flange covers at the upper end and the lower end and communicated with the reaction cylinder body, and the distributor is located at the upper portion of the reaction cylinder body, welded on the inner wall of the outer flange cover at the upper end and right opposite to the inlet tube. The ceramic foam layer is arranged inside the reaction cylinder body. The portable ethanol self-heating hydrogen production reactor can realize the fact that raw material is evenly distributed on catalyst surface, ethanol conversion rate is more than 90 percent, and hydrogen selectivity exceeds 70 percent. The reactor has compact structure, high raw material utilization ratio and high energy density. Good performance of being movable can still be ensured after internal members are installed.
Description
Technical field
The utility model relates to a kind of small-sized self-heating reforming hydrogen manufacturing reactor, can realize that especially raw material is at the equally distributed ethanol reforming hydrogen-preparation reactor of catalytic bed.
Background technology
Along with the development of hydrogen fuel cell technology, require the portable onboard hydrogen source of exploitation.Because ethanol can obtain by the biomass ferment technology, be that the reforming hydrogen producing technology of raw material can reduce CO in present thermochemistry hydrogen producing technology with ethanol
2Clean discharging.The realization of ethanol reformation hydrogen production machine requires to design and develop the high-performance micro hydrogen-manufacturing reactor that matches.
The method of ethanol thermochemistry reformation hydrogen production mainly comprises following 3 classes:
C
2H
5OH+3H
2O → 6H
2+ 2CO
2(reforming reaction SRE, strong heat absorption)
C
2H
5OH+1.5O
2→ 3H
2+ 2CO
2(partial oxidation POE, strong heat release)
C
2H
5OH+0.5O
2+ 2H
2O → 5H
2+ 2CO
2(self-heating recapitalization ATRE, heat release)
SRE can provide higher H
2Yield, but strong heat absorption makes this reaction must adopt the extra power heat supply.For the miniaturization hydrogen making machine, this not only means the complexity of system, and can't break away from the dependence for electrical network or other fuel, is difficult to use in the mobile energy or emergency source of electric power etc.Though POE can address the above problem, the hydrogen yield is lower.Sneak into part oxygen and can take into account the above two advantage in pure water fuel, under suitable metering ratio, exothermic heat of reaction can worked under thermal conditions by maintenance system, thereby need not outer heating, is called self-heating recapitalization.For obtaining portable onboard hydrogen source, must effectively improve reaction efficiency, reduce reactor volume, to improve the travelling performance of reactor.Therefore the self-heating reforming hydrogen manufacturing that does not rely on outside heat supply is comparatively suitable hydrogen manufacturing mode.
Because the progress of processing technology, conversion zone transmits performance and is applied in various fields such as catalyzed oxidation (burning), hydrogenation, reformations with its superior heat, matter at the microreactor of micron to mm-scale.The form of ethanol reformation hydrogen production microreactor mainly comprises based on the plate-type reactor of dull and stereotyped microchannel and the cartridge reactor of integration support of the catalyst such as regular ceramic honey comb of employing or foamed ceramics at present.For the former, up to the present, under low reynolds number (0.1＜Re＜10) condition raw material in the microchannel/research and the design of the distribution performance of the raw material of structural response device inside is comparatively abundant.But for portable ethanol self-heating reforming hydrogen manufacturing reactor, consider the needs of thermal management, reactor need adopt core structure usually.Than plate-type reactor, its characteristics are that the raw material treatment capacity is big, Reynolds number height (100＜Re＜2000), and gas is the flow velocity of reactor inlet higher (per second can reach ten to tens of rice).Because the hydrogen manufacturing performance of microreactor seriously relies on the distribution effect of raw material at catalyst surface, if when carrying out reactor design, consider the work of inlet feed distribution and optimization aspect, can significantly improve reactor performance.The key points in design of this inlet distribution mechanism should fully adapt to the characteristics of compact mini-reactor, with simple in structure, volume is little, installation is reliable and simple and easy being advisable.Adopted nozzle to the dispersion that atomizes of the reactant (liquid form mixt of second alcohol and water) of inlet in some reports, but atomizing nozzle often needs additional pneumatic shuttle, and structure is comparatively meticulous and complicated, installation difficulty in the microreactor of compact construction is higher, and is not suitable for the situation that the inlet reactant is gas phase steam.
Summary of the invention
The utility model is in the ethanol self-heating reforming hydrogen manufacturing reaction process, reactor air speed height, and the catalyst surface flow velocity is big, and raw material is at the catalytic bed skewness; The reactor turndown ratio is little, amplify the problem of difficulty, provides that a kind of inside reactor feed distribution is even, hydrogen production efficiency is high, compact construction, form simply install.By the inner member (sparger) of ad hoc structure is installed in the feed(raw material)inlet of reactor, can guarantee that reactor has good distribution performance under the prerequisite that is of compact construction.
The utility model adopts the method that obstacle type inner member is installed at reactor inlet, suitably increase the pressure drop of raw material before entering the ceramic foam layer of supported catalyst, reasonably change the flow direction of fluid before entering ceramic foam layer, thereby improve the distribution effect of raw material, improve the hydrogen manufacturing performance of reactor at the ceramic foam laminar surface.
The purpose of this utility model is achieved through the following technical solutions:
A kind of portable ethanol autothermal reactors for hydrogen production comprises reacting cylinder body, in two pairs, the outward flange lid, and inlet or outlet duct, the ceramic foam layer of sparger and supported catalyst; Described reacting cylinder body two ends is up and down all welded the inside flange lid, inside and outside blind flange sealing butt joint, described inlet or outlet duct is welded to the outward flange lid outside of upper/lower terminal respectively and communicates with reacting cylinder body, described sparger is positioned at reacting cylinder body top, and is welded on the outward flange lid inwall of upper end and over against inlet tube; Described ceramic foam layer is located in the reacting cylinder body.
Preferably, the inwall of described reacting cylinder body is provided with quartzy insulating pipe.
Preferably, described ceramic foam layer is separated into two chambers up and down with reacting cylinder body, and the side of ceramic foam layer is close to quartzy insulation tube wall.
Preferably, described ceramic foam layer is fixed in the middle part or the middle and lower part of reacting cylinder body by supporting tube.
Preferably, described sparger is a hemisphere, and hemispheroidal sphere is over against inlet tube, and the vertex distance inlet side outward flange of sphere covers inwall 0.1～3mm.
Preferably, described hemispheroidal diameter is 20%～50% of a reactor shell internal diameter.
Preferably, described sparger is a cone, and the circular cone top is over against inlet tube, and the vertex of a cone is apart from inlet side outward flange lid inwall 0.1～3mm.
Preferably, described cone bottom surface circular diameter is 10%～20% of a reactor shell internal diameter, highly be catalyst layer upper surface and reaction raw materials the inlet distance 10%～15%.
Preferably, between the inwall of described reacting cylinder body and the quartzy insulating pipe Graphite pad is housed also.
Above-mentioned reactor adopts core structure, and by stainless material processing, the inner quartz liner of adding is equipped with Graphite pad to improve the heat-insulating property of reactor between bushing pipe and the metal wall, to prevent that raw material is between the two slit flow mistake.Whole reactor is placed among the incubation chamber, and silica wool is filled in the space of between.Catalyzer places the bottom of reactor, and the mixed air of raw material such as alcohol-water, air enters reactor from inlet tube.Reacted product gas flows out from the pipeline of bottom.The distance of catalyst layer upper surface and reaction raw materials inlet is 70mm.Inner member is installed as sparger in ingress (as drawing the zone of circle among Fig. 1).Ingress and ceramic foam layer upper surface have bigger distance, to promote raw material fully diffusion before arriving ceramic foam layer, uniform distribution on ceramic foam layer.The gas that reaction generates is derived by the outlet pipe of reactor.
The ceramic foam layer of described reactor adopts a kind of ZrO
2The precious metal Ir/La of ceramic foam load
2O
3Catalyzer, it is fixed by quartzy supporting tube in the axial position of reactor.Between catalyst layer and reactor body, be lined with quartzy insulating pipe, to reduce calorific loss.
Compared with prior art the beneficial effects of the utility model are as follows:
(1) reactor of the present utility model can be realized raw material at the catalyst surface uniform distribution, and the catalysis foam bottom surface temperature difference is generally at 10-30 ℃ in the reaction process.Reactor is in the air speed scope of broad (0.1～2 * 10
51/h) have higher self-heating reforming hydrogen manufacturing performance, ethanol conversion is greater than 90%, and hydrogen selective surpasses 70%.And do not add the reactor of any inner member, and its ethanol conversion is lower than 85%, and hydrogen selective is lower than 65%.
(2) structure of reactor compactness of the present utility model, prepared using efficient height, the energy density height can guarantee still behind the inner member of installation that reactor has good travelling performance.
(3) reactor of the present utility model has short reaction start time, after reactor is preheating to 300～400 ℃, reacts start time less than 100s.
(4) reactor of the present utility model has lower pressure drop.
Description of drawings
Fig. 1 is the structural representation that utilizes the semisphere inner member to improve the reactor of feed distribution performance of the present utility model.
Fig. 2 is the enlarged view of semisphere inner member among Fig. 1.
Fig. 3 improves the structural representation of the reactor of feed distribution performance for the conical inner member of utilization of the present utility model.
Fig. 4 is the enlarged view of conical inner member among Fig. 3.
Fig. 5 be among Fig. 1 A-A to sectional view.
Fig. 6 be among Fig. 1 B-B to sectional view.
Embodiment
Below in conjunction with accompanying drawing and specific examples the utility model is described further.
As shown in Figure 1, a kind of portable ethanol autothermal reactors for hydrogen production, reactor adopts core structure, by stainless material processing, comprises reacting cylinder body 1, inlet tube 2, in 8, two pairs of the outlet pipes, outward flange lid 6,5, sparger 3, quartzy supporting tube 7, the ceramic foam layer 4 of quartzy insulating pipe 9 and supported catalyst.
Reacting cylinder body 1 is processed by stainless steel, internal diameter 88mm, and height 120mm, inside flange lid 6 is all welded at two ends.Inside and outside blind flange 6,5 butt joints, and adopt the screw of diameter 6mm to cooperate Graphite pad 10 sealings.Inlet tube 2 and outlet pipe 8 all adopt stainless material processing, are welded on the two outward flanges lid 5 pipeline external diameter 19mm, internal diameter 15mm respectively.Described sparger is that radius is the stainless steel hemisphere of 14mm, and it is welded on the upper end outward flange and covers on 5 inwalls, and sphere is over against inlet tube 2, and the top of sphere is 1mm apart from inlet side outward flange lid inwall.
Reacting cylinder body 1 inner heat-insulating property of adding quartzy insulating pipe 9 with the raising reactor reduces calorific loss.Quartzy insulating pipe external diameter 86mm, internal diameter 82mm.Between the wall of quartzy insulating pipe 9 and reacting cylinder body 1 Graphite pad 12 is housed also, to prevent that raw material is between the two slit flow mistake.
The ceramic foam layer 4 of supported catalyst is to adopt a kind of ZrO
2The precious metal Ir/La of ceramic foam load
2O
3Catalyzer is made diameter 80mm, and height 30mm's is cylindrical, places in the reacting cylinder body 1, and its bottom is fixed by quartzy supporting tube 7.Quartzy supporting tube external diameter 82mm, internal diameter 76mm, length 20mm.The distance of ceramic foam layer 4 upper surfaces and reaction raw materials inlet is 70mm.Inlet has bigger distance with the ceramic foam layer upper surface, to promote raw material fully diffusion before arriving ceramic foam layer, uniform distribution on ceramic foam layer.Whole reactor is placed among the incubation chamber, and silica wool is filled in the space of between.
Charging is ethanol, desalination water and air.Ethanol flow: 100mol/h, discharge 200mol/h, air flow quantity 83mol/h (pressing oxygen flow calculates).Feed pressure: 1.2MPa, feed ethanol and water wiring solution-forming, 300 ℃ of gasifications, air normal temperature sample introduction.Before the reaction, adopt outside electric heating device 11 that ceramic foam layer is preheating to 300 ℃.
The mixed steam of air and ethanol water enters reactor by inlet tube 1, and is mixed and disperse at sparger 3 places, enters ceramic foam layer 4 subsequently.Because the effect of the catalyzer of ceramic foam layer 4 loads, raw material reacts rapidly at catalyst surface, and the ceramic foam layer core temperature is elevated to 650 ℃ in 90s, and stablizing rear center to limit wall temperature difference is 15 ℃, obtains hydrogen-rich gas simultaneously.Reacted product gas flows out from outlet pipe 8.After reaction started, whole system did not need additional heat to supply with.The ethanol conversion 95% of this utility model, hydrogen selective 73%.
The difference of present embodiment and embodiment 1 is:
Described sparger is a cone, and it highly is 8mm, and the conical bottom radius surface is 6mm, and the circular cone top is over against inlet tube, and the vertex of a cone is apart from inlet side outward flange lid inwall 1mm, as shown in Figure 3.
The mixed steam of air and ethanol water enters reactor by inlet tube 1, and is mixed and disperse at sparger 3 places, enters ceramic foam layer 4 subsequently.Because the effect of catalyzer, raw material reacts rapidly at catalyst surface, and the ceramic foam layer core temperature is elevated to 650 ℃ in 95s, and stablizing rear center to limit wall temperature difference is 50 ℃, obtains hydrogen-rich gas simultaneously.Reacted product gas flows out from outlet pipe 8.After reaction started, whole system did not need additional heat to supply with.The ethanol conversion 91% of this utility model, hydrogen selective 70%.
The present embodiment difference from Example 1 is that the radius of semisphere sparger 3 is 10mm.
The ethanol conversion 93% of this utility model, hydrogen selective 73%.
The present embodiment difference from Example 1 is that the radius of semisphere sparger 3 is 20mm.
The ethanol conversion 91% of this utility model, hydrogen selective 72%.
The foregoing description is a preferred implementation of the present invention; but embodiments of the present invention are not restricted to the described embodiments; other any do not deviate from change, the modification done under spirit of the present invention and the principle, substitutes, combination, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (9)
1. a portable ethanol autothermal reactors for hydrogen production is characterized in that, comprises reacting cylinder body, in two pairs, the outward flange lid, and inlet or outlet duct, the ceramic foam layer of sparger and supported catalyst; Described reacting cylinder body two ends is up and down all welded the inside flange lid, inside and outside blind flange sealing butt joint, described inlet or outlet duct is welded to the outward flange lid outside of upper/lower terminal respectively and communicates with reacting cylinder body, described sparger is positioned at reacting cylinder body top, and is welded on the outward flange lid inwall of upper end and over against inlet tube; Described ceramic foam layer is located in the reacting cylinder body.
2. reactor according to claim 1 is characterized in that the inwall of described reacting cylinder body is provided with quartzy insulating pipe.
3. reactor according to claim 2 is characterized in that, described ceramic foam layer is separated into two chambers up and down with reacting cylinder body, and the side of ceramic foam layer is close to quartzy insulation tube wall.
4. reactor according to claim 3 is characterized in that, between the inwall of described reacting cylinder body and the quartzy insulating pipe Graphite pad is housed also.
5. according to claim 1 or 2 or 3 or 4 described reactors, it is characterized in that described ceramic foam layer is fixed in the middle part or the middle and lower part of reacting cylinder body by supporting tube.
6. reactor according to claim 5 is characterized in that, described sparger is a hemisphere, and hemispheroidal sphere is over against inlet tube, and the vertex distance inlet side outward flange of sphere covers inwall 0.1～3mm.
7. reactor according to claim 6 is characterized in that, described hemispheroidal diameter is the reactor shell internal diameter
20％～50％。
8. reactor according to claim 5 is characterized in that, described sparger is a cone, and the circular cone top is over against inlet tube, and the vertex of a cone is apart from inlet side outward flange lid inwall 0.1～3mm.
9. reactor according to claim 8 is characterized in that, described cone bottom surface circular diameter is 10%～20% of a reactor shell internal diameter, highly be catalyst layer upper surface and reaction raw materials the inlet distance 10%～15%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120147490XU CN202089764U (en) | 2011-05-10 | 2011-05-10 | Portable ethanol self-heating hydrogen production reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120147490XU CN202089764U (en) | 2011-05-10 | 2011-05-10 | Portable ethanol self-heating hydrogen production reactor |
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| Publication Number | Publication Date |
|---|---|
| CN202089764U true CN202089764U (en) | 2011-12-28 |
Family
ID=45364845
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120147490XU Expired - Fee Related CN202089764U (en) | 2011-05-10 | 2011-05-10 | Portable ethanol self-heating hydrogen production reactor |
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| Country | Link |
|---|---|
| CN (1) | CN202089764U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104437275A (en) * | 2014-11-12 | 2015-03-25 | 宁夏嘉翔自控技术有限公司 | Fluidized bed reactor for solar hydrogen production system |
| CN106378067A (en) * | 2015-08-04 | 2017-02-08 | 中国石化工程建设有限公司 | Axial micro-catalytic reaction unit and application thereof |
-
2011
- 2011-05-10 CN CN201120147490XU patent/CN202089764U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104437275A (en) * | 2014-11-12 | 2015-03-25 | 宁夏嘉翔自控技术有限公司 | Fluidized bed reactor for solar hydrogen production system |
| CN106378067A (en) * | 2015-08-04 | 2017-02-08 | 中国石化工程建设有限公司 | Axial micro-catalytic reaction unit and application thereof |
| CN106378067B (en) * | 2015-08-04 | 2019-04-26 | 中国石化工程建设有限公司 | A kind of micro- catalysis reaction member of axial direction and application thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20111228 Termination date: 20140510 |