CN101016992A - Combustion device for low concentration gaseous hydrocarbon - Google Patents
Combustion device for low concentration gaseous hydrocarbon Download PDFInfo
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- CN101016992A CN101016992A CN 200710020394 CN200710020394A CN101016992A CN 101016992 A CN101016992 A CN 101016992A CN 200710020394 CN200710020394 CN 200710020394 CN 200710020394 A CN200710020394 A CN 200710020394A CN 101016992 A CN101016992 A CN 101016992A
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Abstract
The invention relates to a burner with low-density gas hydrocarbon, characterized in that an annular air inlet channel and a discharge channel with multiple rings are formed by thin annular outer wall and inner wall to form bidirectional reverse airflow channel to communicate with a burning room at the center of the annular channel, the burning room contains a porous material, the heat transmission is realized between the inlet and outlet airflow channels in the annular airflow channel, to avoid transmitting heat between the gas and heat medium in present reactor and avoid side heat hurt on wall. And when the airflow channels are enough, the inventive device can reach higher working temperature to reduce the density limit of burning more, without steering airflow and using catalyst timely. The invention has low thermal insulation demand to simplify the device and reduce cost. The invention can use the low-density gas hydrocarbon as natural gas or the like.
Description
Technical field:
The invention belongs to the combustion apparatus technical field, particularly the burner of coalmine ventilation low concentration gas gas.
Background technology:
China's " industry security and environmental protection " (2002,28 (3) 3-5 page or leaf) introduced hot-fluid changes reactor (Thermal Flow-Reversal Reactor, operation principle TFRR).This reactor is divided into three layers, and middle one deck is a heat exchanger, but two outside layers is by quartz sand or ceramic particle efficient storage that constitutes and the heat exchange medium layer that transmits heat.When bringing into operation, earlier one deck heat exchange medium is wherein carried out preheating by heating, make it reach required about of Device in Gas burning temperature more than 1000 ℃, feed coal mine to ventilate mash gas gas then, heat is transferred to gas from heat exchange medium, gas is heated and reaches the temperature required generation oxidation reaction of burning, emit heat, emit the part heat through the heat exchanger layer, arrive another layer heat exchange medium then and most of heat is transferred to it, the heat of storage burning back gas is to keep the bulk temperature of combustion chamber.Under the prerequisite that burning is kept, control transfer of heat particularly by gas to the efficiency limitations among others of the heat transmission course of solid the maximum temperature of reactor; If temperature is too high, then Outlet Gas Temperature is too high, and heat of taking away and wall heat loss sum are if surpassed combustion heat product, and temperature of reactor can descend; Because heat ceaselessly is transferred to another layer by gas from one deck heat exchange medium in the reactor, originally the heat exchange medium layer temperature of high temperature can constantly reduce, and another layer temperature can constantly raise, when the temperature of elevated temperature heat exchange media layer is reduced to when maybe can not keep burning, need change the direction of air-flow back and forth from top to bottom and from bottom to top, make the combustion zone transfer to another layer heat exchange medium layer, so repeatedly, therefore need regular airflow-reversing, cause the device structure complexity; To keep heat exchange medium, around the reactor good heat insulation layer need be arranged for fear of a large amount of heat radiations more than 1000 ℃.
" Chinese coal " (2003,29 (11), the 11-12 page or leaf) introduced the catalysis matchmaker bidirectional flow reactor that Canadian mineral products and Inst Energiteknik (CANMET) develop (Catalytic Flow-ReversalReactor, CFRR).Its structural design and operational mode and above-mentioned TFRR are basic identical, only have been to use catalyst to reduce the ignition temperature of combustion gas.Though burning is more easily taken place,, has increased the complexity of equipment owing to introduced catalyst layer.Efficient storage that TFRR uses causes the regular airflow-reversing of the limited needs of temperature of reactor to cause complex structure and the shortcoming that the well insulated layer need be arranged with the heat exchange medium layer of transmission heat, still exists in CFRR.
Summary of the invention:
The invention provides a kind of burner of low concentration gaseous hydrocarbon, to overcome the above-mentioned shortcoming of prior art.
The burner of low concentration gaseous hydrocarbon of the present invention comprises airflow inlet 7 and outlet 4, porous material 15 and the electrical heating elements 19 that places in it; It is characterized in that: surround the gas channel that ring-type inlet channel 12 and exhaust passage 14 form bidirectional adverse current by lamellar outside wall surface 8 and internal face 9, be communicated with the combustion chamber 16 that is positioned at annular channel circle center; Combustion chamber 16 is built-in with porous material 15.
Low concentration gaseous hydrocarbon of the present invention is meant the gaseous hydrocarbon of mean concentration between 0.03～3% (its suitable combustion concentration limit can be different for different types of gaseous hydrocarbon), is meant especially to contain the methane mean concentration at 0.2～0.75% coalmine ventilation low concentration gas gas.
Can be in a plurality of parts that the combustion chamber are divided into connection around the wall stationary barrier 11 of combustion chamber 16; Usually adopt 1 to 3 dividing plate the combustion chamber to be divided into 2 to 4 parts that are interconnected; The length of dividing plate 11 is no more than 90% of combustion chamber 16 diameters; But separator material is selected the material of 1300～1800 ℃ of heatproofs for use, comprises high-alumina brick, silica brick, complex silicon carbide, magnesia brick or corundum.
Described gas channel can adopt the multi-turn gas channel of helical form, circular or square ring-type, adopts the 3-25 circle usually, this number of turns be meant lamellar internal face 9 around the number of turns; Can be provided with fixed support rod 13 between described lamellar outside wall surface 8 and the internal face 9.
The described volume of the interior porous material 15 in combustion chamber 16 that places is advisable to account for 16 spaces 5～100%, combustion chamber; Can be equipped with temperature thermocouple 10 in this porous material 15.
During use, the porous material 15 that starts earlier in 19 pairs of combustion chambers of electrical heating elements 16 is preheating to above the required temperature of low concentration gaseous hydrocarbon burning, feed low concentration gaseous hydrocarbon from airflow inlet 7 then, enter combustion chamber 16 contact porous materials 15 through ring-type inlet channel 12, heat is transferred to low concentration gaseous hydrocarbon from porous material 15 and makes it to reach the temperature required back generation of burning oxidation reaction, emits heat; Air communication after the burning is crossed combustor exit 18 and is entered exhaust passage 14, discharges by outlet 4 again; When entering operate as normal, after the air-flow of low concentration fuel gas enters and surrounds inlet channel 12 by lamellar outside wall surface 8 and internal face 9, the high-temperature exhaust air that is deflated in the passage 14 heats through the heat exchange of thin plate wall, enter combustion chamber 16 from combustion chamber import 17 then, the porous material 15 and finish combustion process of flowing through at this.The present invention takes the round gas channel setting of bidirectional adverse current, and purpose is the heat transmission that realizes between the turnover air-flow; Filling porous material 15 in combustion chamber 16, purpose are the stability of strengthening burning.
Because the present invention has taked the round gas channel of bidirectional adverse current, the round that heat is transmitted in bidirectional adverse current is imported and exported between the gas channel wall and is realized, avoided existing hot-fluid to change the gas of reactor employing and the heat transmission course between the heat exchange medium, avoided the side heat waste of wall simultaneously, therefore when airflow channels is abundant, this device can reach higher operating temperature, thereby can further reduce the concentration limit of burning; Because the heating of gas is carried out in gas channel among the present invention, avoided heat to be transferred to the process of another layer by gas from one deck heat exchange medium, the high-temperature region can not shifted, and does not therefore need regularly to carry out airflow-reversing to keep burning, thereby simplified equipment, reduced cost; Because the round airflow channel structure of the bidirectional adverse current that the present invention takes can be ignored the side heat waste of device, the heat loss of device is little, thereby requires lower to outside heat insulation layer; Thereby both simplified equipment, and reduced cost.
Changeing reactor with existing hot-fluid compares, the porous material 15 that the present invention adopts only places a part in the combustion chamber, storage and transmission to heat only help out, purpose is to strengthen the stability of burning, thereby the material quantity that uses is few and low to its performance requirement,, maintenance requirement is also lower, and its cost changes reactor with hot-fluid and compares minimum; Adding dividing plate among the present invention in the combustion chamber, mainly is to make burning more stable, has also avoided the incomplete combustion that may occur simultaneously.
In a word, because the burner of low concentration gaseous hydrocarbon of the present invention has been taked the round gas channel of bidirectional adverse current, compare with existing apparatus, can reach higher operating temperature, can further reduce the concentration limit of burning, need not regular airflow-reversing and catalyst simultaneously, require low external insulation, simplify equipment, reduced cost.Burner of the present invention is applicable to comprising the oil reservoir gas in coal mine to ventilate mash gas gas, natural gas, biogas, the Petroleum Production or the low concentration gaseous hydrocarbon of the combustible exhaust gas in the Chemical Manufacture.
Description of drawings:
Fig. 1 is that circular, dividing plate number is the example structure schematic diagram of 1 low concentration gaseous hydrocarbon burner for gas channel of the present invention.
Fig. 2 is that gas channel is that helical form, dividing plate number are the example structure schematic diagram of 2 low concentration gaseous hydrocarbon burner.
Fig. 3 is that the gas channel side of being ring-type, dividing plate number are the example structure schematic diagram of 1 low concentration gaseous hydrocarbon burner.
The specific embodiment:
Further specify the specific embodiment of the burner of low concentration gaseous hydrocarbon of the present invention below in conjunction with accompanying drawing.
Embodiment 1:
The gas channel that Fig. 1 has provided the burner of present embodiment low concentration gaseous hydrocarbon is the enforcement structural representation of annulus: the inlet channel 12 and the exhaust passage 14 that are surrounded the multi-turn annular by lamellar outside wall surface 8 and internal face 9, form the gas channel of bidirectional adverse current, be communicated with the combustion chamber 16 that is positioned at annular channel circle center.Desirable 3 to 25 circles of the number of turns of general gas channel, the number of turns less than 3 o'clock control transfer of heat amounts a little less than, and too high greater than 25 o'clock costs, lose more than gain.
In the present embodiment, in the combustion chamber, from outside wall surface, extend two parts that a dividing plate 11 is divided into combustion chamber 16 connection, the length of dividing plate is 70% of combustion chamber 16 diameters, and generally its length does not surpass 90% of combustion chamber diameter, the oversize circulation that can influence air-flow; Dividing plate in the present embodiment uses the compound carbofrax material manufacturing.Can between lamellar outside wall surface 8 and internal face 9, be provided with fixed support rod 13, with play fix two distances between plates from the effect of supporting.Inlet channel 12 is communicated with combustion chamber 16 through combustion chamber import 17.For smooth combustion, in combustion chamber 16, be equipped with porous material 15.16 volumes that are built-in with porous material 15 account for 20% of 16 spaces, combustion chamber in the combustion chamber in the present embodiment; Usually can influence the stability of burning if porous material is less than 5%, along with the increase of the shared combustion chamber volume ratio of porous material, the stability of burning can be strengthened, and the ratio of the shared combustion chamber of porous material can be no more than 50% to save material generally speaking; As required, porous material also rises to 100%, and be the multi-hole medium combustion state this moment; At porous material 15 in-built electrical heating element heaters 19, and temperature thermocouple 10 can be set simultaneously.Combustion chamber 16 is communicated with exhaust passage 14 by combustor exit 18, is in communication with the outside through exporting 4 again; Inlet channel 12 communicates with blower fan 5 and coalmine ventilation gas source of the gas 1 by import 7 simultaneously, and gas table 3 is installed at import 7 places.
During use, start electrical heating elements 19 earlier, for igniting successfully, this moment, air intake valve 2 and blower fan valve 6 kept closing, when reaching more than 1000 ℃, the temperature that temperature thermocouple 10 records opens air intake valve 2, the low concentration gas gas 1 of coalmine ventilation enters combustion chamber 16 by import 7 through ring-type inlet channel 12, contact porous material 15, blower fan valve 6 is still closed at this moment, after about 10 minutes, heat is transferred to low concentration gaseous hydrocarbon from porous material 15 and makes it to reach the temperature required about oxidation reaction that afterwards takes place more than 1000 ℃ of burning, emits heat, closes electrical heating this moment; High-temperature gas passes combustor exit 18 enters exhaust passage 14,12 gas transmission heat in inlet channel; After device enters normal operating conditions, the exhaust airstream that charge air flow is deflated in the passage in the inlet channel 12 is warming up to more than 1000 ℃ through lamellar partition heat transfer, enter combustion chamber 16 by combustion chamber import 17, smooth combustion under the booster action of porous material 15 storages and transmission heat, high-temperature gas after the burning is given porous material 15 with part heat transmission storage on the one hand, enter exhaust passage 14 through combustor exit 18 simultaneously, with 12 the gas transmission in inlet channel of most of heat, discharge from exporting 4 at last.
Arresting stop when work, cut off air-flow earlier and supply with, open valve 6 again with air purge gas channel 5 minutes.
Can be provided with or not be provided with dividing plate in the combustion chamber of the burner of low concentration gaseous hydrocarbon of the present invention.
Be provided with under the situation of using a dividing plate 11, the air-flow U-shaped path of flowing through in the combustion chamber can make the combustible gas of not combustion and the heat-exchange time lengthening of high temperature combustion gas and porous material like this, has increased the stability of burning; Combustible gas is elongated in the time of staying of combustion chamber, the situation of effectively having avoided unburned fully just to be drained.In the ordinary course of things, the piece number of dividing plate is advisable between 1 to 3, causes complex structure in meeting too much, increases maintenance difficulties, and cost increases.
Because the concentration that the gas in the coalmine ventilation gas is gushed out has certain fluctuation, when change in concentration surpasses certain limit, can influence the operational effect of device, even cause stopping working, therefore be preferably in air inlet installation gas table 3 and monitor, show gas density at any time.During operation, surpass 1.5%, then start blower fan 5 if gas table 3 shows gas density, open blower fan valve 6, ventilate to the charge air flow passage, the gas density that shows up to gas table 3 is in 0.2～0.75% scope, close blower fan valve 6 again, stop the operation of blower fan 5; If gas table 3 shows that gas density is lower than 0.1%, then start electrical heating elements 19, when the gas density of gas table 3 demonstration is in 0.2～0.75% scope, stop electrical heating.
Because the present invention has taked the round gas channel of bidirectional adverse current, heat is transmitted between import and export air-flow in the round gas channel of bidirectional adverse current and realizes, avoid existing hot-fluid to change the gas of reactor and the heat transmission course between the heat exchange medium, avoided the side heat waste of wall simultaneously; Therefore, when airflow channels was abundant, this device can reach higher operating temperature, thereby can further reduce the concentration limit of combustion gas; Because the heating of gas is carried out in gas channel among the present invention, avoided heat to be transferred to the process of another layer by gas from one deck heat exchange medium, the high-temperature region can not shifted, and does not therefore need the regular airflow-reversing to keep burning, thereby simplified equipment, reduced cost; Because the round airflow channel structure of the bidirectional adverse current that the present invention takes can be ignored the side heat waste of device, the heat loss of device is little, thereby lower to outside heat insulation layer requirement, thereby has both simplified equipment, and has reduced cost.
Built-in porous material helps out with storage and transmission to heat the present invention's employing in the combustion chamber, purpose is to strengthen the stability of burning, thereby change reactor with existing hot-fluid and compare used quantity much less, performance requirement to material is also lower, maintenance requirement is also lower, and its cost changes reactor with hot-fluid and compares minimum.
Compare with existing catalysis matchmaker bidirectional flow reactor, because the present invention has taked the round gas channel of bidirectional adverse current, can reach higher operating temperature, under the auxiliary storage of the porous material of in the combustion chamber, filling and the effect of transmission heat, not need the catalyst gas-flow easily to burn.
The burner of low concentration gaseous hydrocarbon of the present invention be according to the gas mean concentration in the China's coal-mine ventilation gas generally the present situation between 0.2～0.75% design.If the number of turns that the gas mean concentration not between 0.2～0.75%, only needs to change this height of devices or changes gas channel can reach combustion purpose.That discharges in the annual coalmine ventilation gas of China does not have treated gas up to 15,000,000,000 standard cubic meters, its greenhouse effects surpass the discharge capacity of the greenhouse gases in the Holland whole nation, caused the serious environmental pollution, if the coal mine to ventilate mash gas gas firing can be utilized, then can not only obtain to be equivalent to the energy of at least 1,000 ten thousand tons of standard coals, also its greenhouse effects be reduced to below 1/20.
The main component methane of the gas in the coalmine ventilation is that carbon number is 1 gaseous hydrocarbon.Burner of the present invention is for also being suitable for the gaseous hydrocarbon under a part of carbon number that different ratios combines less (generally being no more than 4), the normal temperature and pressure by carbon, two kinds of elements of hydrogen, except that coal mine to ventilate mash gas gas, also comprise the oil reservoir gas in natural gas, biogas, the Petroleum Production, the combustible exhaust gas in the Chemical Manufacture, their main component all is a gaseous hydrocarbon.
Burner of the present invention different types of low concentration gaseous hydrocarbon that can burn.Low concentration gaseous hydrocarbon (methane as 0.2～0.75%) is which kind of gaseous hydrocarbon acts as a fuel and all can not change the hot rerum natura of charge air flow substantially because its quality proportion is little, different gaseous hydrocarbons, and just ignition temperature is different with mole combustion heat.When fuel gas was not methane, according to its ignition temperature difference, only needing increased or reduces a few circle gas channels, just can change the heating-up temperature that charge air flow reaches, and is heated to the ignition temperature of this gaseous hydrocarbon under the corresponding concentration and burning can be proceeded; The difference of the mole combustion heat just makes the concentration limit difference of its burning, and for example for low concentration propane, the concentration limit of burning under the situation that increases airflow channels can arrive below 0.04%; And for methane, its burning concentration limit can only arrive 0.08% after the increase airflow channels.
Embodiment 2:
Present embodiment is that gas channel is that helical form and dividing plate number are 2 situation.
Fig. 2 is the structural representation of present embodiment: present embodiment adopts the helical form gas channel, adopts 2 dividing plates 11 that the combustion chamber is separated into 3 zones in combustion chamber 16, and the length of each dividing plate is 70% of combustion chamber diameter.Other is identical with embodiment 1.
Helical form gas channel good effect of heat exchange, the stream pressure loss is little, but processing is difficult; During work, air-flow is separated into the S type path of flowing through in 3 zones by 2 dividing plates in combustion chamber 16, enter exhaust passage 14 again and discharge by outlet 4, and this structure can make the heats transmission in the combustion chamber 16 and the time lengthening of combustion reaction, thereby combustion stability is better, makes burning more complete.
Embodiment 3:
Present embodiment is the situation of the gas channel side of being ring-type.
Fig. 3 is the structural representation of present embodiment: the inlet channel 12 and the exhaust passage 14 of lamellar outside wall surface 8 and internal face 9 side's of surrounding ring-types.Other is with embodiment 1.This side's annular flow passage is compared with the helical form gas channel with circular gas channel, and its stream pressure loss is bigger, but device is easy to processing, can reduce cost.
Claims (8)
1, a kind of burner of low concentration gaseous hydrocarbon comprises airflow inlet (7) and outlet (4), porous material (15) and place its interior electrical heating elements (19); It is characterized in that: surround ring-type inlet channel (12) and exhaust passage (14) by lamellar outside wall surface (8) and internal face (9), form the gas channel of bidirectional adverse current, be communicated with the combustion chamber (16) that is positioned at annular channel circle center; Combustion chamber (16) is built-in with porous material (15).
2, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that described low concentration gaseous hydrocarbon is meant the gaseous hydrocarbon of mean concentration between 0.03～3%.
3, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that described low concentration gaseous hydrocarbon is to contain the methane mean concentration at 0.2～0.75% coal mine to ventilate mash gas gas.
4, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that fixing 1 to 3 dividing plate (11) around the wall of combustion chamber (16) combustion chamber to be divided into 2 to 4 parts of connection; The length of dividing plate (11) is no more than 90% of combustion chamber (16) diameter; But separator material is selected the material of 1300～1800 ℃ of heatproofs that comprise high-alumina brick, silica brick, complex silicon carbide, magnesia brick or corundum for use.
5, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that described gas channel adopts the multi-turn gas channel of 3-25 circle helical form, circular or square ring-type.
6, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that between described lamellar outside wall surface (8) and the internal face (9) to be provided with fixed support rod (13).
7, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that the described volume of the interior porous material (15) in combustion chamber (16) that places accounts for 5～100% of the bags.
8, the burner of gaseous hydrocarbon as claimed in claim 1 is characterised in that the porous material (15) of described combustion chamber (16) is built-in with temperature thermocouple (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100203947A CN100485260C (en) | 2007-02-15 | 2007-02-15 | Combustion device for low concentration gaseous hydrocarbon |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100203947A CN100485260C (en) | 2007-02-15 | 2007-02-15 | Combustion device for low concentration gaseous hydrocarbon |
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| CN101016992A true CN101016992A (en) | 2007-08-15 |
| CN100485260C CN100485260C (en) | 2009-05-06 |
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| CNB2007100203947A Expired - Fee Related CN100485260C (en) | 2007-02-15 | 2007-02-15 | Combustion device for low concentration gaseous hydrocarbon |
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Cited By (7)
| 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 |
| CN101531336B (en) * | 2009-04-17 | 2011-04-06 | 合肥工业大学 | Small-sized high efficiency self-heating natural gas hydrogen-preparing device |
| CN103278599A (en) * | 2013-03-25 | 2013-09-04 | 广东电网公司电力科学研究院 | Low-density gas burner, burning test system and controlling method thereof |
| CN104841255A (en) * | 2014-02-13 | 2015-08-19 | 许鸣铁 | Double spiral electric heating gas oxidation decomposition device |
| GB2582912A (en) * | 2019-04-02 | 2020-10-14 | Edwards Ltd | Burner |
| CN112370967A (en) * | 2020-11-19 | 2021-02-19 | 安徽燃博智能科技有限公司 | Self-heating catalytic oxidation device |
| CN112717684A (en) * | 2020-12-17 | 2021-04-30 | 安徽燃博智能科技有限公司 | Coiled plate type self-heating catalytic oxidizer |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2240071A1 (en) * | 1972-08-16 | 1974-02-28 | Otto Dipl Ing Brust | Incinerator for odorous vapours - with spiral recuperator for thermal econ-omy |
| DE2824946A1 (en) * | 1978-06-07 | 1979-12-20 | Eisenmann Kg Maschinenbau Ges | Combustion equipment avoiding obnoxious components - mixes preheated oxygen-deficient oxidant with fuel at inlet to combustion chamber with heat-radiating quartz glass rods |
| DE2908912A1 (en) * | 1979-03-07 | 1980-09-18 | Mueller Otto Gmbh | Burner removing organic gas or vapour from crude contaminated air - has combustion chamber at centre of interleaved-spiral-sheet counterflow heat exchanger |
| CN2596663Y (en) * | 2002-12-20 | 2003-12-31 | 清华大学 | Device based on fuel burning for directly realizing heat-electic changing |
| CN1322598C (en) * | 2005-01-07 | 2007-06-20 | 清华大学 | Counterflow heat exchanging burners |
| CN201021800Y (en) * | 2007-02-15 | 2008-02-13 | 中国科学技术大学 | A combustion device for low-thickness gas hydrocarbon |
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2007
- 2007-02-15 CN CNB2007100203947A patent/CN100485260C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101531336B (en) * | 2009-04-17 | 2011-04-06 | 合肥工业大学 | Small-sized high efficiency self-heating natural gas hydrogen-preparing device |
| 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 |
| CN103278599A (en) * | 2013-03-25 | 2013-09-04 | 广东电网公司电力科学研究院 | Low-density gas burner, burning test system and controlling method thereof |
| CN104841255A (en) * | 2014-02-13 | 2015-08-19 | 许鸣铁 | Double spiral electric heating gas oxidation decomposition device |
| GB2582912A (en) * | 2019-04-02 | 2020-10-14 | Edwards Ltd | Burner |
| CN112370967A (en) * | 2020-11-19 | 2021-02-19 | 安徽燃博智能科技有限公司 | Self-heating catalytic oxidation device |
| CN112717684A (en) * | 2020-12-17 | 2021-04-30 | 安徽燃博智能科技有限公司 | Coiled plate type self-heating catalytic oxidizer |
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| CN100485260C (en) | 2009-05-06 |
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Granted publication date: 20090506 Termination date: 20110215 |