CN1663908A - Natural gas pyrolysis reactor for solid oxide fuel battery - Google Patents
Natural gas pyrolysis reactor for solid oxide fuel battery Download PDFInfo
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- CN1663908A CN1663908A CN2004100135927A CN200410013592A CN1663908A CN 1663908 A CN1663908 A CN 1663908A CN 2004100135927 A CN2004100135927 A CN 2004100135927A CN 200410013592 A CN200410013592 A CN 200410013592A CN 1663908 A CN1663908 A CN 1663908A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
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Abstract
The invention provides a reactor for natural gas cracking of the solid oxide fuel battery, which is middle or small in size for fuel gas production. The reactor support is fixed at the lower part of the outer tube of the reactor, the reaction tube is in the middle of the reactor, the two ends are connected with the large and small tube plate both on the left and right separately, the left and right closure head is securely connected with the outer tube separately through flange. The inlet port for stock is arranged on the left closure head while the outlet for production is arranged on the right closure head. The reactor is vacuum formed with the electric-heat wire in flush type and characterized by the uniform temperature in the reactor and low investment cost, furthermore, it is easy and simple to handle and amplified. The invention is suitable for preparing synthetic gas with multiple reformed petrifaction fuel, the crack can be methane, natural gas, cracked petroleum gas and so on, which supply fuel gas for solid oxide fuel battery of thousands of watts.
Description
(1) technical field:
The present invention proposes a kind of natural gas pyrolysis reactor that is used for Solid Oxide Fuel Cell, specifically, is to be used for the middle-size and small-size reactor that fuel gas is produced, and this fuel gas is used for Solid Oxide Fuel Cell.
(2) background technology:
The fuel gas main component of natural gas pyrolysis reactor production is a synthetic gas.The reactor and the method for producing synthetic gas are that people are known.Early stage conversion of natural gas preparing synthetic gas adopts non-catalytic partial oxidation technology mostly, progressively replaced afterwards by steam reforming technology, because the energy consumption of steam reforming technology is bigger, developed again and united confession thermal conversion process and catalytic oxidation process, and catalyzing part oxidation is not applied to the production of large-scale industry yet.
Solid Oxide Fuel Cell (SOFC) be the 4th generation fuel cell, synthetic gas acts as a fuel, and to directly apply to SOFC be feasible to gas.In view of fuel characteristic and the hot conditions of SOFC, fuel gas directly enters the SOFC negative pole under high-temperature condition.But steam reformation needs a large amount of energy consumptions that steam and supply response heat absorption are provided, and a large amount of water vapour are arranged in the product gas, and entering the SOFC negative pole can influence electrode performance and battery efficiency.In the confession thermal reforming gas a large amount of water vapour is also arranged.The temperature of reaction of non-catalytic partial oxidation is very high, reactor material is required harsh.Catalyzing part oxidation is gentle thermopositive reaction, catalyzing part oxidation system hydrogen-enriched fuel gas, and with its specific efficiency height mutually, energy consumption is low, has tangible economic and social benefit.
(3) summary of the invention:
The present invention proposes a kind of reactor that can satisfy middle-size and small-size intermediate temperature solid oxide fuel cell combustion gas demand.The characteristics of this reactor are shell and tube (many pipes), temperature unanimity radially in the holding tube.Another characteristics of the present invention are that electrically heated starts.Reaction stops electrically heated after reaching stable state, relies on self heat release of reaction, makes reaction proceed.
The present invention mainly is made up of Reaktionsofen support 1, terminal stud 2, reaction tube 3, thermopair 4, left end socket 5, right end socket 6, raw material inlet mouth 9, product air outlet 10, thermal insulation material 12, inner barrel 13, outer cylinder body 14, left side tubule plate 15, left side large tubesheet 16, right side tubule plate 17, right side large tubesheet 18, wherein answer furnace cradle 1 to be connected with reactor outer cylinder body 14 by welding, be used to support reactor, and be positioned on the experiment table.Reaction tube 3 left ends float with reactor left side tubule plate 15 and are connected, and fixedly connected with left side large tubesheet 16; Reaction tube 3 right-hand members float with the right side tubule plate 17 of reactor and are connected, and fixedly connected with right side large tubesheet 18, load catalyzer in the heat district 11 of reaction tube 3, as catalytic partial oxidation reaction.Electrical heating wire is embedded in the inner barrel 13, be used for to reaction tube 3 heating, the length of its winding is longer slightly than heat district 11, nichrome wire is drawn by the terminal stud 2 of outer cylinder body 14 bottom righthand sides that are positioned at reactor, the external temperature controller, thermopair 4 is installed in the middle part, top of the outer cylinder body 14 of reactor, be used to measure temperature, the temperature that thermopair 4 is directly measured is the tubulation surface temperature, because bore is less, can ignore radial temperature difference, records temperature and be pipe inner catalyst bed temperature, raw material gas inlet 9 is installed in the centre of left end socket 5, product gas outlet 10 is installed in the centre of right end socket 6, and the outer cylinder body of left end socket 5 and right end socket 6 and reactor 14 is connected by flange seal, forms left air chamber 7] and right air chamber 8, thermal insulation material 12 has good insulation effect, can make the reactor surface temperature be lower than 100 ℃.Reaction tube 3 becomes equilateral triangle to arrange in inner barrel 13.1 one-tenth saddle type of Reaktionsofen support, two terminal studs 2 are welded on the outer cylinder body 14, are respectively the positive pole and the negative poles of the nichrome wire of being drawn by inner barrel 13, and two terminal studs 2 are external in the positive and negative electrode of external power.
Be described in detail principle of work of the present invention below: with the Sweet natural gas is example, enter reactor before, Sweet natural gas at first with oxygen mix.Start reactor, during temperature programming controlling reactor temperature to the 500 ℃ left and right sides, feed Sweet natural gas oxygen mix fuel gas in reactor, reactor continues to be warming up to 700 ℃.Propellant combination gas enters left air chamber 7 by raw material gas inlet 9, enters reaction tubes 3 again, can enter reaction zone through one section preheating from left side large tubesheet 16 to heat district 11.In heat district 11, partial oxidation reaction takes place in propellant combination gas on catalyzer, and this reaction is thermopositive reaction.Product gas is drawn by the product gas outlet 10 on the right end socket 6 through right air chamber 8, enters the negative pole of SOFC.Question response carry out for some time stable after, stop electrically heated, the liberated heat of reaction own makes reaction proceed.
Major advantage of the present invention is to adopt embed type nichrome wire vacuum forming well heater to give tubulation whole heating, and temperature deploys to ensure effective monitoring and control of illegal activities evenly, and thermocouple temperature measurement is controlled automatically.Heating zone length can be determined according to unstripped gas composition and synthetic gas consumption.For with a kind of raw material, when operational condition is constant, change catalyst consumption, can change combustion gas output.Feed stock conversion and gas production rate are different because of the difference of catalyzer.
(4) description of drawings:
Fig. 1 is a principle of the invention structure iron.
Fig. 2 is the sectional view of Fig. 1 along the I-I line.
Fig. 3 be Fig. 1 along the II-II line left view.
(5) embodiment:
According to the gas quantity of multikilowatt intermediate temperature solid oxide fuel cell needs, be raw material with the Sweet natural gas, with maximum (the 10L/min H that needs combustion gas
2+ CO); Productive rate minimum quantity (methane conversion 80%, H
2, the CO selectivity is respectively 90% and 85%): for condition is carried out the process that reactor is determined in technological design, the boiler tube length overall is 550mm, and heating zone 150mm arranges 7 pipes, and internal diameter is 8mm, external diameter 10mm.The tubulation material is selected for use has oxidation-resistance and anti-CH
4, H
2, the corrosive Cr25Ni20 of CO.
Increase catalyst consumption in the production test, or change catalyst performance, can increase gas production rate.Satisfy the needs that Solid Oxide Fuel Cell is amplified.The fuel gas that this reactor is produced can make multikilowatt intermediate temperature solid oxide fuel cell steady running 1000h, and its battery efficiency is all more than 70%.
Embodiment 1:
Use Ni content is 12% Ni/Al
2O
3, (20-60 order) catalyzer, 4.2g is sub-packed in seven reaction tubes altogether.Under the condition of 108000ml/ (g.h), after the reaction, methane conversion is 84%, H
2, the CO selectivity is respectively 92% and 86%, combustion gas (H
2+ CO) output is 9.8L/min.More than the continuously-running 1200h, battery efficiency 72%.
Embodiment 2:
Use Ni content to be 1%Ni-Ce/Al as 11%Ce content
2O
3(20-60 order) catalyzer, 4.2g is sub-packed in seven reaction tubes altogether.Keep the condition of air speed 108000ml/ (g.h) constant, after the reaction, methane conversion is 85%, H
2, the CO selectivity is respectively 94% and 87%, combustion gas (H
2+ CO) output is 10.0L/min.More than the continuously-running 1200h, battery efficiency is 74%.
Claims (2)
1. natural gas pyrolysis reactor that is used for Solid Oxide Fuel Cell is characterized in that:
Mainly by Reaktionsofen support [1], terminal stud [2], reaction tube [3], the left end socket of thermopair [4] [5], right end socket [6], raw material inlet mouth [9], product air outlet [10], thermal insulation material [12], inner barrel [13], outer cylinder body [14], left side little tube sheet [15], left side large tubesheet [16], the little tube sheet in right side [17], right side large tubesheet [18] is formed, wherein Reaktionsofen support [1] is connected with reactor outer cylinder body [14] by welding, be used to support reactor, and be positioned on the experiment table, reaction tube [3] left end floats with the reactor little tube sheet in left side [15] and is connected, fixedly connected with left side large tubesheet [16], the right-hand member of reaction tube [3] floats with the little tube sheet in the right side of reactor [17] and is connected, fixedly connected with right side large tubesheet [18], in the heat district [11] of reaction tube [3], load catalyzer, electrical heating wire is embedded in the inner barrel [13], be used for heating to reaction tube [3], the length of its winding is longer slightly than heat district [11], nichrome wire is drawn by the terminal stud [2] of the outer cylinder body that is positioned at reactor [14] lower-left end, the external temperature controller, thermopair [4] is installed in the middle part of reactor outer cylinder body [14] top, raw material gas inlet [9] is installed in the centre of left end socket [5], product gas outlet [10] is installed in the centre of right end socket [6], left side end socket [5] is connected by flange seal with the outer cylinder body [14] of reactor with right end socket [6], form left air chamber [7] and right air chamber [8], reaction tube [3] becomes equilateral triangle to arrange in inner barrel [13], Reaktionsofen support [1] becomes the saddle type, two terminal studs [2] are welded on the outer cylinder body [14], be respectively the positive pole and the negative pole of the nichrome wire of being drawn by inner barrel [13], two terminal studs [2] are external in the positive and negative electrode of external power.
2. reactor according to claim 1 is characterized in that: reaction tube [3] is some.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100135927A CN1256272C (en) | 2004-03-03 | 2004-03-03 | Natural gas pyrolysis reactor for solid oxide fuel battery |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100135927A CN1256272C (en) | 2004-03-03 | 2004-03-03 | Natural gas pyrolysis reactor for solid oxide fuel battery |
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| Publication Number | Publication Date |
|---|---|
| CN1663908A true CN1663908A (en) | 2005-09-07 |
| CN1256272C CN1256272C (en) | 2006-05-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100135927A Expired - Fee Related CN1256272C (en) | 2004-03-03 | 2004-03-03 | Natural gas pyrolysis reactor for solid oxide fuel battery |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102826507A (en) * | 2012-08-24 | 2012-12-19 | 华南理工大学 | Method and device of hydrogen production by natural gas and steam reforming for micro fuel cells |
| CN101500939B (en) * | 2006-08-08 | 2014-05-28 | 乔治洛德方法研究和开发液化空气有限公司 | Production and processing unit for a synthesis gas comprising a steam reformer |
| CN104319411A (en) * | 2014-11-10 | 2015-01-28 | 夏伟绩 | Electrode pad pressure balancing energy storage device with multiple air chambers and multiple poles |
-
2004
- 2004-03-03 CN CNB2004100135927A patent/CN1256272C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101500939B (en) * | 2006-08-08 | 2014-05-28 | 乔治洛德方法研究和开发液化空气有限公司 | Production and processing unit for a synthesis gas comprising a steam reformer |
| CN102826507A (en) * | 2012-08-24 | 2012-12-19 | 华南理工大学 | Method and device of hydrogen production by natural gas and steam reforming for micro fuel cells |
| CN102826507B (en) * | 2012-08-24 | 2014-12-31 | 华南理工大学 | Method and device of hydrogen production by natural gas and steam reforming for micro fuel cells |
| CN104319411A (en) * | 2014-11-10 | 2015-01-28 | 夏伟绩 | Electrode pad pressure balancing energy storage device with multiple air chambers and multiple poles |
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| Publication number | Publication date |
|---|---|
| CN1256272C (en) | 2006-05-17 |
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