CN101838557B - Coal gas producer and coal gas production method - Google Patents
Coal gas producer and coal gas production method Download PDFInfo
- Publication number
- CN101838557B CN101838557B CN2010101095119A CN201010109511A CN101838557B CN 101838557 B CN101838557 B CN 101838557B CN 2010101095119 A CN2010101095119 A CN 2010101095119A CN 201010109511 A CN201010109511 A CN 201010109511A CN 101838557 B CN101838557 B CN 101838557B
- Authority
- CN
- China
- Prior art keywords
- coal
- zone
- reduction
- oxidation zone
- gas generator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The invention discloses a coal gas producer and a coal gas production method. The coal gas producer comprises a producer body, wherein the producer body comprises an oxidation zone and a reduction zone therein; the oxidation zone is communicated with a coal inlet and an air inlet, the coal inlet and the air inlet are respectively filled with coal and air for combustion oxidation reaction, so that carbon dioxide can be generated; the reduction zone is communicated with a reduction coal inlet, and reduction reaction is carried out on reduction coal introduced from a reduction coal inlet and carbon dioxide generated from combustion to generate carbon monoxide. In the technical scheme of the invention, the combustion oxidation reaction and reduction reaction during the coal gas production reaction process are respectively and fully carried out, and temperature can be respectively controlled to promote the oxidation reaction and the reduction reaction to be carried out fully, thereby improving the combustion efficiency of coal and reducing resource consumption.
Description
Technical field
The embodiment of the invention relates to the gas production equipment and technology, relates in particular to a kind of producer gas generator and coal gas production method.
Background technology
Producer gas generator is to be the common equipment of feedstock production coal gas with the coal.The typical structure of existing producer gas generator comprises body of heater 1 as shown in Figure 1, and body of heater 1 lower end comprises air distribution plate 2, and air distribution plate 2 upsides are communicated with coal inlet 3, and air distribution plate 2 downsides are vaporization agent import 4.The coal dust that feeds from coal inlet 3 comprises multiple particle diameter, for example 10mm, 6mm, 3mm and 1mm are following several, coal dust is passed on the air distribution plate 2, and vaporization agent sprays into from bottom to top from the through hole 5 of air distribution plate 2 downsides by air distribution plate 2, makes that the incendiary coal dust is blown to raise in the whole producer gas generator.Because coal particle size is inconsistent, so coal dust layering in body of heater 1 suspends.The position that heavier pulverized coal particle is kicked up is low, and the position of lighter pulverized coal particle oxygen is higher, and cinder proportion is bigger and burn completely, can be deposited on the air distribution plate 2, falls by the through hole on the air distribution plate 25, thereby discharges residue.Be provided with export mouth 6 in the upper end of producer gas generator, the gas mixture that reaction generates and the coal dust of small particle size together export to cyclonic separator 7.Through the centrifugation of cyclonic separator 7, gas mixture is separated with coal dust, gas mixture is derived, and coal dust is led go back to the position of air distribution plate 2 annexes along return line 8, continues participation and burns.
In existing producer gas generator, the main reaction that the coal combustion heat release takes place in zone of next-door neighbour's air distribution plate upside, temperature is approximately 1200 ℃.For preventing the too high problem that causes coking and blocking of temperature of combustion, on the basis of required coal of burning and oxygen suitable proportion, need to feed excessive coal, lower the temperature with the reduction reaction between coal and carbonic acid gas and the water vapour.Generate carbon monoxide and hydrogen by reduction reaction, this is the major ingredient of required coal gas in gas mixture.
In carrying out research process of the present invention, the contriver finds that the existing defective of above-mentioned producer gas generator is: burning of coal efficient is low, and is not energy-conservation.Owing to carry out the reaction of combustion oxidation and reduction cooling in fact simultaneously in the combustion zone, so the ratio between the coal of in fact uncontrollable participation incendiary coal and participation oxidation, most of coal does not have perfect combustion.
Summary of the invention
The embodiment of the invention provides a kind of producer gas generator and coal gas production method, to improve burning of coal efficient, reduces resource consumption.
The embodiment of the invention provides a kind of producer gas generator, comprises body of heater, wherein: comprise oxidation zone and reduction zone in the described body of heater; Described oxidation zone is communicated with coal inlet and inlet mouth, and coal that described coal inlet and inlet mouth feed respectively and air carry out the combustion oxidation reaction, to generate carbonic acid gas; Described reduction zone with go back the raw coal import and be communicated with, describedly go back the raw coal of going back that the raw coal import feeds and carry out reduction reaction, to generate carbon monoxide with the described carbonic acid gas that burning generates.
Wherein, described oxidation zone is above described reduction zone;
Described reduction zone comprises throat neck section and pressure release section, and described throat neck section is connected with described oxidation zone, and the cross-sectional area of described throat neck section is respectively less than the cross-sectional area of described oxidation zone and described pressure release section; Described going back on the wall that the raw coal import is arranged on described throat neck section.
Aforesaid producer gas generator, also be provided with cowling panel in the preferably described oxidation zone, the below that described cowling panel is arranged on described inlet mouth cuts off described oxidation zone, and described cowling panel is provided with a plurality of via holes, and described coal inlet extends to described cowling panel place through conduit and exposes.
Aforesaid producer gas generator, preferably the lower end of described reduction zone is communicated with export mouth, is used to derive the residue behind described carbon monoxide and the coal combustion; The export mouth of described producer gas generator is connected to a storage receptacle.
Aforesaid producer gas generator, preferably described quantity of going back the raw coal import is a plurality of, circumferentially is evenly distributed on the wall of described reduction zone.
Aforesaid producer gas generator, preferably the coal inlet of described oxidation zone and inlet mouth are injecting combustor.
The embodiment of the invention also provides a kind of coal gas production method that uses the producer gas generator that the foregoing description provides, and comprising:
Oxidation zone to producer gas generator feeds coal and air, carries out the combustion oxidation reaction in described oxidation zone, to generate carbonic acid gas;
Feed in the reduction zone that is connected with described oxidation zone and to go back raw coal, describedly go back raw coal, with the generation carbon monoxide with described carbonic acid gas carries out reduction reaction;
The coal that feeds to the oxidation zone of producer gas generator be coal slurry or with water vapour for carrying the fine coal of coal medium.
Aforesaid coal gas production method, preferably the temperature of described oxidation zone is at least 1200 ℃, perhaps more preferably is more than 1500 ℃.
Technical scheme of the present invention is as much as possible independently carried out combustion oxidation reaction and reduction reaction that coal gas reacts in the process.Feed enough air in oxidation zone, coal is fully burnt.In the reduction zone, because going back raw coal, feeding increased reducing agents, make reduction reaction occupy main status, the cooling effect that cooling effect when also raw coal feeds and reduction reaction heat absorption cause all makes and is difficult to proceed burning in the reduction zone, thereby can form relatively independent oxidation zone and reduction zone in the producer gas generator of one, promotes oxidn and reduction reaction are carried out separately fully.Thereby improved burning of coal efficient, reduced consumed resource.
Description of drawings
Fig. 1 is the structural representation of existing producer gas generator;
The structural representation of the producer gas generator that Fig. 2 provides for the embodiment of the invention one;
The structural representation of a kind of producer gas generator that Fig. 3 provides for the embodiment of the invention;
The structural representation of the another kind of producer gas generator that Fig. 4 provides for the embodiment of the invention;
The structural representation of another producer gas generator that Fig. 5 provides for the embodiment of the invention;
The schema of the coal gas production method that Fig. 6 provides for the embodiment of the invention two.
Embodiment
For the purpose, technical scheme and the advantage that make the embodiment of the invention clearer, below in conjunction with the accompanying drawing in the embodiment of the invention, technical scheme in the embodiment of the invention is clearly and completely described, obviously, described embodiment is the present invention's part embodiment, rather than whole embodiment.Based on the embodiment among the present invention, those of ordinary skills belong to the scope of protection of the invention not making the every other embodiment that is obtained under the creative work prerequisite.
Embodiment one
The structural representation of the producer gas generator that Fig. 2 provides for the embodiment of the invention one, this producer gas generator comprises body of heater 1.Comprise oxidation zone 10 and reduction zone 20 in the body of heater 1.Oxidation zone 10 is communicated with coal inlet 3 and inlet mouth 11, feed coal from coal inlet 3, be preferably the feeding coal slurry, perhaps also can feed fine coal for carrying the coal medium by water vapour, from inlet mouth 11 bubbling airs, make coal slurry and air carry out the combustion oxidation reaction, even part moisture content is arranged in the coal slurry, because suitably control amount of oxygen and temperature also can make coal burn fully.Reduction zone 20 with go back raw coal import 21 and be communicated with, go back raw coal import 21 and be used for feeding and go back raw coal, for example be coal slurry or coal dust etc.Also raw coal carries out reduction reaction with the carbonic acid gas that burning generates, to generate carbon monoxide.
In the present embodiment, the coal inlet 3 and the inlet mouth 11 of oxidation zone 10 are preferably injecting combustor, make coal that coal inlet 3 feeds can be as much as possible fully, rapid combustion, temperature can reach at least 1200 ℃, perhaps more preferably is more than 1500 ℃.Can further design the shape, position relation of coal inlet 3, inlet mouth 11, oxidation zone 10 etc., make to form turbulent flow rationally in the oxidation zone 10, it is more abundant to burn.
For example, can be as shown in Figure 3, the inlet end that coal inlet 3 is set stretches within the oxidation zone 10, thereby the position of producing coal can be enclosed among the air fully, coal is fully contacted with air burn.
Again or, as shown in Figure 4, inlet mouth 11 can be designed as the admission passage 110 of arc shape, then compressed or non-pressurized space can form certain eddy current after admission passage 110 sprays into oxidation zone, the having of eddy current helps make coal particle and Air mixing more even, thereby promotes burning.Admission passage 110 is not limited to be camber line shape, can also be spirrillum etc.
As shown in Figure 5, can also be provided with cowling panel 12 in the oxidation zone 10, the below that cowling panel 12 is arranged on inlet mouth 11 cuts off oxidation zone 10, and cowling panel 12 is provided with a plurality of via holes, through hole just, supplied gas circulation.Coal inlet 3 extends to cowling panel 12 places through conduit 13 and exposes.Being provided with of cowling panel 12 cuts off into oxidation zone 10 on two zones, bubbling air in the upper area of cowling panel 12, form bigger pressure, pass less via hole and be squeezed into lower part of oxidation zone 10, both improved the flow velocity of air-flow, and made the uneven air-flow homogenizing in cowling panel 12 tops pass cowling panel 12 again.Coal inlet 3 extends to cowling panel 12 places through conduit 13 and exposes, and makes the outlet position of coal be in the encirclement of even high velocity air, helps burning more.
Rectification to air inlet is not limited to control the air current flow rule by improving admission passage, for example can also come rectification by the shape of design oxidation zone 10, make air-flow spray into oxidation zone 10 backs and under the guiding of oxidation zone 10 walls, form eddy current, promote uniform mixing, thereby promote burning.
The technical scheme of present embodiment is as much as possible independently carried out combustion oxidation reaction and reduction reaction that coal gas reacts in the process, and the temperature in oxidation zone 10 and the reduction zone 20 has obvious variation.Feed enough air in oxidation zone 10, coal is fully burnt, so because the abundant oxidizing reaction of oxygen occupies main status.In the reduction zone 20, because going back raw coal, feeding increased reducing agents, make reduction reaction occupy main status, the cooling effect that cooling effect when also raw coal feeds and reduction reaction heat absorption cause all makes and is difficult to proceed burning in the reduction zone 20, thereby can form relatively independent oxidation zone 10 and reduction zone 20 in the producer gas generator of one.
In the present embodiment, the quantity of going back raw coal import 21 is preferably a plurality of, circumferentially is evenly distributed on the wall of reduction zone 20.Make and go back raw coal and enter more evenly, reduction reaction is more abundant.
The reason that oxidation zone and reduction zone are independently separated be can the combustion reactions of promotes oxidn district fully carry out the temperature in controlled oxidation district independently, thereby feeding amount that can be by control coal and air and improve temperature and promote burning.Compare with reduction zone blended scheme with the prior art oxidation zone, when the incendiary coal has concurrently when carrying out reduction reaction, reduction reaction is absorbed heat in a large number, causes that temperature reduces, burning is insufficient.Therefore, the technical scheme of present embodiment can effectively improve burning of coal efficient, reduces resource consumption.
In the present embodiment, oxidation zone 10 preferably is set as shown in Figure 2 above reduction zone 20.Certain the present invention is not limited to shown in Figure 2, and for example, oxidation zone 10 is connected setting with the level that reduction zone 20 can also walk abreast, and perhaps reduction zone 20 is arranged on oxidation zone 10 tops, sets up on the wall of reduction zone 20 and goes back raw coal import 21.
Present embodiment adopts oxidation zone to be in the advantage of last technical scheme, the coal slurry or the fine coal of high-temp combustion are in flow state, behind the absorbing and cooling temperature of reduction zone, can solidify coking, in the technical scheme of present embodiment, the cinder mixture of flow state can fall under action of gravity, can coking and blocking.
The shape of reduction zone 20 can have certain volumetrical shape for the cylindric of equal diameters or other, preferably designs cylindric that reduction zone 20 do not wait for diameter in the present embodiment.Reduction zone 20 comprises throat neck section 22 and pressure release section 23, and throat neck section 22 is connected with oxidation zone 10, and the cross-sectional area of throat neck section 22 makes producer gas generator form the thick middle thin shape in two ends respectively less than the cross-sectional area of oxidation zone 10 and pressure release section 23.Also raw coal import 21 is arranged on the wall of throat neck section 22.
Adopt technique scheme, carbonic acid gas that combustion reactions obtains and heat all can significantly improve density in the less circulation area of throat neck section 22, feed herein again and go back raw coal, and reduction reaction can take place rapidly, fully.Pressure release section 23 next-door neighbour's throat neck sections 22, the carbon monoxide that makes reaction generate can flow out rapidly.Unburning material residue etc. can spread rapidly, avoids stopping up throat neck section 22.
In the present embodiment, the place of leading of carbon monoxide mouth 6 is arranged on reduction zone 20, and the export mouth 6 of residue can optionally be arranged on the lower end of body of heater 1 according to the relative position relation of oxidation zone 10 and reduction zone 20.When oxidation zone 10 was arranged on the top of reduction zone 20, preferably 20 lower end was communicated with export mouth 6 in the reduction zone, was used to derive the residue behind carbon monoxide and the coal combustion.Oxidation zone 10 is arranged on the top of reduction zone 20, makes a large amount of heat energy to fall along with residue, thereby for reduction zone 20 provides high temperature energy, is difficult for taking place coking.Export mouth 6 preferably adopts the body that favours horizontal plane, and being easy to derives residue.
Producer gas generator of the present invention, export mouth 6 can also be connected to a storage receptacle, for example employing existing producer gas generator as shown in Figure 1 is as storage receptacle, a plurality of producer gas generators of the present invention can be connected in the storage receptacle, can pressure release, storage, and can further unburnt coal in the residue be led back from coal inlet 3, avoid resources loss.
The technical scheme that the embodiment of the invention provided is distinguished oxidation zone 10 and reduction zone 20, makes oxidizing reaction and reduction reaction relatively independent, can control respectively, makes reaction more abundant.And oxidation zone 10 and reduction zone 20 can be arranged in the body of heater 1, be spaced from each other to go back raw coal import 21, the absorbing and cooling temperature effect by reduction reaction makes combustion reactions carry out the transition to reduction reaction rapidly, and reactant circulation distance is short, it is smooth and easy to circulate, and power loss is few.And distinguish oxidation zone 10 and reduction zones 20 to go back raw coal import 21, and make it be formed at being also advantageous in that in the whole body of heater 1 and be convenient on existing body of heater 1, transform, be convenient to popularization, cost is low.
Embodiment two
The schema of the coal gas production method that Fig. 6 provides for the embodiment of the invention two, the producer gas generator that this method can adopt the embodiment of the invention to provide is carried out, and comprising:
Step 610, feed coal and air, carry out the combustion oxidation reaction in oxidation zone, to generate carbonic acid gas to the oxidation zone of producer gas generator;
Step 620, feed in the reduction zone that is connected with oxidation zone and to go back raw coal, go back raw coal and carbonic acid gas and carry out reduction reaction, with the generation carbon monoxide.
The method of present embodiment is carried out oxidizing reaction and reduction reaction relatively independently, therefore can oxidizing reaction and reduction reaction be carried out separately fully by control reactant concn and reaction zone temperature, has improved reaction efficiency.
In concrete the application, the temperature of oxidation zone is at least 1200 ℃, perhaps more preferably is more than 1500 ℃, fully to burn.The coal that feeds to the oxidation zone of producer gas generator be preferably coal slurry or with water vapour for carrying the fine coal of coal medium, adhere to body of heater when avoiding dry coal dust to feed body of heater and stop up.In oxidation zone generation reduction reaction, can feed the air capacity of oxidation zone though feed coals such as coal slurry can contain certain moisture content, make the combustion oxidation reaction occupy main status, make coal obtain abundant oxidation by control.
It should be noted that at last: above embodiment only in order to technical scheme of the present invention to be described, is not intended to limit; Although with reference to previous embodiment the present invention is had been described in detail, those of ordinary skill in the art is to be understood that: it still can be made amendment to the technical scheme that aforementioned each embodiment put down in writing, and perhaps part technical characterictic wherein is equal to replacement; And these modifications or replacement do not make the essence of appropriate technical solution break away from the spirit and scope of various embodiments of the present invention technical scheme.
Claims (7)
1. a producer gas generator comprises body of heater, it is characterized in that: comprise oxidation zone and reduction zone in the described body of heater; Described oxidation zone is communicated with coal inlet and inlet mouth, and coal that described coal inlet and inlet mouth feed respectively and air carry out the combustion oxidation reaction, to generate carbonic acid gas; Described reduction zone with go back the raw coal import and be communicated with, describedly go back the raw coal of going back that the raw coal import feeds and carry out reduction reaction, to generate carbon monoxide with the described carbonic acid gas that burning generates;
Described oxidation zone is above described reduction zone;
Described reduction zone comprises throat neck section and pressure release section, and described throat neck section is connected with described oxidation zone, and the cross-sectional area of described throat neck section is respectively less than the cross-sectional area of described oxidation zone and described pressure release section; Described going back on the wall that the raw coal import is arranged on described throat neck section.
2. producer gas generator according to claim 1, it is characterized in that: also be provided with cowling panel in the described oxidation zone, the below that described cowling panel is arranged on described inlet mouth cuts off described oxidation zone, described cowling panel is provided with a plurality of via holes, and described coal inlet extends to described cowling panel place through conduit and exposes.
3. producer gas generator according to claim 1 is characterized in that: the lower end of described reduction zone is communicated with export mouth, is used to derive the residue behind carbon monoxide and the coal combustion; The export mouth of described producer gas generator is connected to a storage receptacle.
4. producer gas generator according to claim 1 is characterized in that: described quantity of going back the raw coal import is a plurality of, circumferentially is evenly distributed on the wall of described reduction zone.
5. producer gas generator according to claim 1 is characterized in that: the coal inlet of described oxidation zone and inlet mouth are injecting combustor.
6. a coal gas production method that uses the described producer gas generator of claim 1 is characterized in that, comprising:
Oxidation zone to producer gas generator feeds coal and air, carries out the combustion oxidation reaction in described oxidation zone, to generate carbonic acid gas;
Feed in the reduction zone that is connected with described oxidation zone and to go back raw coal, describedly go back raw coal, with the generation carbon monoxide with described carbonic acid gas carries out reduction reaction;
The coal that feeds to the oxidation zone of producer gas generator be coal slurry or with water vapour for carrying the fine coal of coal medium.
7. coal gas production method according to claim 6 is characterized in that: the temperature of described oxidation zone is at least 1200 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101095119A CN101838557B (en) | 2010-02-10 | 2010-02-10 | Coal gas producer and coal gas production method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101095119A CN101838557B (en) | 2010-02-10 | 2010-02-10 | Coal gas producer and coal gas production method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101838557A CN101838557A (en) | 2010-09-22 |
| CN101838557B true CN101838557B (en) | 2011-09-21 |
Family
ID=42742235
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010101095119A Active CN101838557B (en) | 2010-02-10 | 2010-02-10 | Coal gas producer and coal gas production method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101838557B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103131476B (en) * | 2011-11-30 | 2017-03-15 | 上海麦风微波设备有限公司 | A kind of microwave manufacturing technique method of coal gas and device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1031103A (en) * | 1987-07-31 | 1989-02-15 | 北京钢铁学院 | A kind of gasification method of fluidizing power coal |
| CN101063053A (en) * | 2007-05-14 | 2007-10-31 | 佛山市科达能源机械有限公司 | Circulating fluidized bed gas generator system |
| CN101063050A (en) * | 2007-05-14 | 2007-10-31 | 佛山市科达能源机械有限公司 | Coal gas production method |
| EP2239312A1 (en) * | 2008-01-29 | 2010-10-13 | Mitsubishi Heavy Industries, Ltd. | Method of starting coal gasification furnace and startup device therefor |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2487737Y (en) * | 2001-07-23 | 2002-04-24 | 云南省昭通地区农业机械化技术推广站 | Solid fuel gasification furnace |
| WO2008082967A1 (en) * | 2006-12-26 | 2008-07-10 | Nucor Corporation | Pyrolyzer furnace apparatus and method for operation thereof |
| CN201704291U (en) * | 2010-02-10 | 2011-01-12 | 马鞍山科达洁能有限公司 | Gas generator |
-
2010
- 2010-02-10 CN CN2010101095119A patent/CN101838557B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1031103A (en) * | 1987-07-31 | 1989-02-15 | 北京钢铁学院 | A kind of gasification method of fluidizing power coal |
| CN101063053A (en) * | 2007-05-14 | 2007-10-31 | 佛山市科达能源机械有限公司 | Circulating fluidized bed gas generator system |
| CN101063050A (en) * | 2007-05-14 | 2007-10-31 | 佛山市科达能源机械有限公司 | Coal gas production method |
| EP2239312A1 (en) * | 2008-01-29 | 2010-10-13 | Mitsubishi Heavy Industries, Ltd. | Method of starting coal gasification furnace and startup device therefor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101838557A (en) | 2010-09-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9296962B2 (en) | System and process for gasifying biomass products | |
| CN203668319U (en) | Biomass gasifying device | |
| CN101575527B (en) | Biomass direct thermal cracking generator and cracking method thereof | |
| CN101760243B (en) | Three-phase multi-material three-dimensional pressurized clash coal gasification device and process thereof | |
| CN103666580A (en) | Coupled biomass pressurized pyrolysis process and system | |
| CN102134512A (en) | Staged powder spraying entrained bed gasification furnace and gasification method thereof | |
| CN106824001A (en) | A kind of device of two-stage biological matter hydro-thermal catalytic activation reaction | |
| CN201704291U (en) | Gas generator | |
| US9328301B2 (en) | Injector and method for co-feeding solid and liquid fuels | |
| CN102249229A (en) | Process using flotation process for preparing activated carbon with high specific surface area by fly ash | |
| CN108758642A (en) | A kind of gasified combustion apparatus | |
| CN101838557B (en) | Coal gas producer and coal gas production method | |
| CN103868055A (en) | Regenerative combustion device applicable to stable combustion of compounded tangent-flow and direct-flow gas with low calorific value | |
| CN204455026U (en) | Combined type circulating fluidized-bed gasification reaction unit | |
| CN101307259B (en) | Gas producing device and method | |
| CN202484984U (en) | Circulating fluidized bed biomass boiler for compressing air and sprinkling fuels | |
| CN109181771A (en) | A kind of catalytic coal gasifaction method and catalytic coal gasifaction device | |
| CN105733685B (en) | Biomass gasifying furnace | |
| CN211170602U (en) | Biomass carbonization material production device | |
| CN208620355U (en) | A kind of gasified combustion apparatus | |
| CN106957057A (en) | A kind of calcium carbide furnace system of hydrogen and oxygen mixed injection and heat integration | |
| CN204607937U (en) | A kind of coal gasification reaction device | |
| CN101963348B (en) | Biomass gas burning system | |
| CN103289751A (en) | Method and device for preparing combustible gas by utilizing biomass | |
| CN102311810A (en) | Method and device for high-temperature melting and gasifying biomass |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: KEDA CLEAN ENERGY (MA ANSHAN) CO., LTD. Free format text: FORMER NAME: MA ANSHAN KEDA CLEAN ENERGY CO., LTD. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 243041 Anhui city in Ma'anshan province north of the revitalization of economic and Technological Development Zone, Road No. 555 Patentee after: KEDA INDUSTRIAL CO., LTD. Address before: 243041 Anhui city in Ma'anshan province north of the revitalization of economic and Technological Development Zone, Road No. 555 Patentee before: Ma'anshan Keda Clean Energy Co., Ltd. |