CN202203950U - Organic solid waste pyrolyzation and gasification device - Google Patents
Organic solid waste pyrolyzation and gasification device Download PDFInfo
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- CN202203950U CN202203950U CN2011202636102U CN201120263610U CN202203950U CN 202203950 U CN202203950 U CN 202203950U CN 2011202636102 U CN2011202636102 U CN 2011202636102U CN 201120263610 U CN201120263610 U CN 201120263610U CN 202203950 U CN202203950 U CN 202203950U
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- rotary kiln
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Abstract
Provided is an organic solid waste pyrolyzation and gasification device, which belongs to the technical field of renewable energy. The pyrolysis chamber adopts a rotary kiln pyrolysis chamber which inclines downwardly. The rotary kiln pyrolysis chamber is provided with a pyrolysis material feeding inlet, a heat carrier inlet, an after-pyrolysis gas mixture outlet, and a solid products outlet. The pyrolysis material feeding inlet is connected to a pyrolysis material feeding device. The heat carrier inlet is connected to the bottom of a first cyclone separator. The organic solid waste pyrolyzation and gasification device is advantageous in that with the adoption of a rotary kiln furnace, no steam or other gaseous fluidization is used, and thereby energy is saved; new materials and heat carrier are uniformly mixed and heat exchange capability is enhanced; the stay time of raw material in a pyrolyzer is controllable, and thereby the pyrolysis reaction can be more thorough; the new material and heat carrier are respectively sent to the furnace from the same end of the rotary kiln furnace, and thereby operation and control are facilitated; the organic solid waste pyrolyzation and gasification device can be used for the pyrolysis gasification of biomass, house refuse and other organic solid waste.
Description
Technical field
The utility model relates to a kind of pyrolysis gasifying device, relates in particular to a kind of pyrolysis gasifying device like organic solid wastes such as living beings, house refuses.
Background technology
Pyrolytic technique is organic solid waste (like living beings, house refuse etc.) to be converted into be convenient to the fuel gas storing, transport; To improve the efficient of using energy source; And help reducing the discharging of pollutant; With direct burning mutually specific energy more can be efficiently, cleaning utilize the energy, more and more receive the attention of countries in the world in recent years.The fuel gas gas main component that the organic solid waste pyrolysis is produced is H
2, CO, CH
4And C
nH
mDeng fuel gas, its calorific value is higher, can be used as industry or domestic fuel, and application prospect is more wide.
Existing organic solid waste pyrolysis processing technology adopts the oxygen debt combustion system of single burner hearth more, and the air capacity of promptly sending into the combustion chamber is about 1/3rd of theoretical air requirement, and the mist that is produced is exactly a fuel gas with low heat value.Mostly this mode is small-sized stove, and difficulty is used for commercial scale.Another kind is to adopt double bed pyrolytic gasification mode, and under this mode, mostly the combustion chamber is fluid bed, and the pyrolysis chamber adopts moving bed, fluid bed or waterfall fluidized bed (column plate bed) more.Need feed fluidizing agent when adopting fluid bed, for example steam or purification back combustion gas, this all can cause the waste of the energy; Select moving bed or waterfall fluidized bed for use, wayward again by the pyrolysis material with mixing of heat carrier with the time of staying.The difficult point of organic solid waste pyrolysis processing technology is: one, how to provide pyrolytic reaction required heat; Two, how to strengthen heat exchange in the pyrolysis oven.Present existing pyrolysis installation does not also well solve these two problems, has limited the further promotion and application of pyrolytic technique to a certain extent.Therefore the more advanced organic solid waste pyrolytic gasification technology of exploitation is very necessary with device.
The utility model content
The purpose of the utility model provides a kind of novel organic solid waste pyrolysis gasifying device, to solve energy waste and the uppity problem that the gasification of available technology adopting double bed is brought.
The technical scheme of the utility model is following:
The utility model is realized through following technical scheme: a kind of organic solid waste pyrolysis gasifying device, contain fluidized bed combustion chamber, heat carrier charging gear, first cyclone separator, waste heat boiler, pyrolysis chamber, pyrolysis material charging gear, second cyclone separator, air preheater and cleaning system; The gas approach of described first cyclone separator links to each other with the exhanst gas outlet of fluidized bed combustion chamber, and the top exhanst gas outlet of first cyclone separator is connected with waste heat boiler through pipeline; The top gas outlet of second cyclone separator is connected with air preheater through pipeline; It is characterized in that: described pyrolysis chamber adopts the rotary kiln pyrogenation chamber; This rotary kiln pyrogenation chamber is tilted to down layout, mixed gas outlet after being respectively equipped with the import of pyrolysis material feed, heat carrier import, pyrolysis on the rotary kiln pyrogenation chamber and solid product outlet; The import of described pyrolysis material feed is connected with described pyrolysis material charging gear; The heat carrier import is connected with the bottom of first cyclone separator; Mixed gas outlet after the pyrolysis links to each other with the inlet of second cyclone separator through pipeline, and the solid product outlet is connected with the emulsion zone of fluidized bed combustion chamber through heat-resisting auger.
The centre of gyration axis of the described rotary kiln pyrogenation of the utility model chamber and the angle of horizontal plane are 3 °～5 °.Described air preheater adopts heat pipe preheater.
The utlity model has following advantage and beneficial effect: 1. adopt rotary kiln as the pyrolysis chamber, the pyrolysis material because gyration and heat carrier mix, has effectively strengthened the heat exchange in the stove in the pyrolysis chamber; 2. need not to feed fluidizing agent, good energy-conserving effect; 3. the time of staying lacks, and is easy to control, and pyrolysis rate is high.4. utilize hot auger loopback thermal decomposition product, improved the reliability of system; 5. pyrolysis processing process continuity is strong, and treating capacity is big, is convenient to realize industrialization promotion, is specially adapted to the extensive pyrolytic gasification of living beings, house refuse and other organic solid waste, for urban life usefulness gas and fuel gas generation provide source of the gas.
Description of drawings
Fig. 1 is the overall structure sketch map of a kind of organic solid waste pyrolysis gasifying device of providing of the utility model.
Among the figure: the 1-fluidized bed combustion chamber; 2-first cyclone separator; 3-rotary kiln pyrogenation chamber; The 4-waste heat boiler; 5-combustion chamber air-introduced machine; The 6-chimney; 7-second cyclone separator; The 8-air preheater; The 9-cleaning system; 10-pyrolysis chamber air-introduced machine; The 11-air accumulator; The 12-pressure fan; 13-heat carrier charging gear; 14-pyrolysis material charging gear; The heat-resisting auger of 15-.
The specific embodiment
Below in conjunction with accompanying drawing the structure and the course of work of the utility model are done further to describe.
Fig. 1 is the overall structure sketch map of a kind of organic solid waste pyrolysis gasifying device of providing of the utility model, and this device contains fluidized bed combustion chamber 1, heat carrier charging gear 13, first cyclone separator 2, waste heat boiler 4, rotary kiln pyrogenation chamber 3, pyrolysis material charging gear 14, second cyclone separator 7, air preheater 8 and cleaning system; The gas approach of described first cyclone separator 2 links to each other with the exhanst gas outlet of fluidized bed combustion chamber, and the top exhanst gas outlet of first cyclone separator is connected with waste heat boiler 4 through pipeline; The top gas outlet of second cyclone separator is connected with air preheater 8 through pipeline; The rotary kiln pyrogenation chamber is tilted to down layout.Mixed gas outlet after being respectively equipped with the import of pyrolysis material feed, heat carrier import, pyrolysis on the rotary kiln pyrogenation chamber and solid product outlet; The import of described pyrolysis material feed is connected with described pyrolysis material charging gear 14; The heat carrier import is connected with the bottom of first cyclone separator 2; Mixed gas outlet after the pyrolysis links to each other with the inlet of second cyclone separator 7 through pipeline, and the solid product outlet is connected with the emulsion zone of fluidized bed combustion chamber 1 through heat-resisting auger 15.
Described fluidized bed combustion chamber is a kind of fast bed combustion chamber, Jiao who is produced by the rotary kiln pyrogenation chamber or the semicoke release heat of burning therein, heat cycles heat carrier; In the effect of carrying secretly of flue gas down, a large amount of solid particles are promoted to top of combustion chamber, leave behind the combustion chamber in cyclone separator separated down, get into rotary kiln pyrogenation chamber 3 and heat the pyrolysis materials.
Described rotary kiln pyrogenation chamber 3 is pyrolysis chambers of the strict pressurized operation of a seal request, and the centre of gyration axis of rotary kiln pyrogenation chamber and the angle of horizontal plane are 3 °～5 °; The pyrolysis material is heated rapidly in the rotary kiln pyrogenation chamber with in the elevated temperature heat carrier mixed process, and pyrolytic reaction takes place, and generates volatile matter gas and solid product Jiao or semicoke; Thermal cyclic carrier after the heat release and as the Jiao or the semicoke particle of thermal decomposition product is sent in the fluidized bed combustion chamber through heat-resisting auger in bottom, rotary kiln pyrogenation chamber.
Said air preheater 8 adopts heat pipe preheater, avoids Direct Air-Cooled to cause tar to condense.
The described heat-resisting auger 15 of the utility model adopts the heat resisting cast steel manufacturings, is a kind of thermal material transport that can operation steady in a long-term under 650 ℃ of conditions.
The said device of the utility model has taken into full account requirements of saving energy, converts the high-temperature flue gas that the combustion chamber produces into saturated vapor through waste heat boiler; The air that the part heat of the high-temperature fuel gas that is generated is used for heating flame chamber needs through heat pipe preheater.
The described device of the utility model has been taked suitable gas-purification measure, and cyclone separator is used for removing the heat ash of combustion gas and sending into heat-resisting auger; Cleaning system comprises spray column, desulfurizing tower and electrical tar precipitator, and the concrete character of looking the pyrolysis material that is equipped with is confirmed with the requirement to combustion gas.
The course of work of the utility model is following:
Pyrolysis material through break process is sent into (temperature of pyrolysis chamber is 650～700 ℃) in the rotary kiln pyrogenation chamber 3 through pyrolysis material charging gear 14; Mix mutually with thermal cyclic carrier at this from the first cyclone separator separator 2; And move forward with the rotation of rotary kiln; Be about 2 minutes by the time of staying of the material of pyrolysis in the rotary kiln pyrogenation chamber, by pyrolysis feed and thermal cyclic carrier rotate and moving process in fully mix and carry out heat exchange, pyrolysis material decomposes; Discharge fuel gas and generate solid-state Jiao or semicoke, the heat of the required absorption of pyrolytic reaction is provided by the high temperature circulation heat carrier.Thermal cyclic carrier after the heat release and pyrogenous origin Jiao or semicoke are flowed out by bottom, rotary kiln pyrogenation chamber, send in the fluidized bed combustion chamber 1 through heat-resisting auger 15.The heat release of in fluidized bed combustion chamber 1, burning of Jiao or semicoke; Make the temperature of combustion chamber reach 850～1000 ℃; The thermal cyclic carrier of 3 inflows is reheated the back and is carried the top that is promoted to fluidized bed combustion chamber 1 by flue gas from the rotary kiln pyrogenation chamber; Separate through first cyclone separator 2 and to get in the rotary kiln pyrogenation chamber 3, get into the rotary kiln pyrogenation chamber with initiate once more after being mixed by pyrolysis feed, form biomass pyrolysis provides heat.Thermal cyclic carrier is according to the above-mentioned flow process flows of going round and beginning again, to keep material balance and heat supply balance.
Pyrogenous origin combustion gas cools to 400 ℃ through air preheater 8 again after 7 dedustings of second cyclone separator, after cleaning system 9 is handled, feed in the air accumulator 11 then.
The high-temperature flue gas that leaves the combustion chamber reclaims heat through afterbody heat-exchange system 4, reduces to the working range that combustion chamber air-introduced machine 5 allows to flue-gas temperature when improving system thermal efficiency, and flue gas enters atmosphere by chimney 6 behind air-introduced machine.
When pyrolysis gasifying device starts; Earlier send into an amount of heat carrier particle (the optional quartz sand that meets size and density requirements, coal ash slag that fluid bed is discharged, haydite etc.) by heat carrier charging gear 13; Send into again and be prone to biomass-burning and light a fire make the indoor normal combustion of fluidized bed combustion; Heat carrier to be recycled starts pyrolysis material charging gear 14 with heating in the rotary kiln pyrogenation chamber 3 and when maintaining 650 ℃, begins the commencement of commercial operation of pyrolytic gasification system to the feeding of rotary kiln pyrogenation chamber.
Because pyrolytic reaction is carried out under the secluding air condition, so fuel gases calorific value is higher, can reach 12MJ.
Claims (3)
1. an organic solid waste pyrolysis gasifying device contains fluidized bed combustion chamber (1), heat carrier charging gear (13), first cyclone separator (2), waste heat boiler (4), pyrolysis chamber (3), pyrolysis material charging gear (14), second cyclone separator (7), air preheater (8) and cleaning system; The gas approach of described first cyclone separator (2) links to each other with the exhanst gas outlet of fluidized bed combustion chamber, and the top exhanst gas outlet of first cyclone separator is connected with waste heat boiler (4) through pipeline; The top gas outlet of second cyclone separator is connected with air preheater through pipeline; It is characterized in that: described pyrolysis chamber adopts rotary kiln pyrogenation chamber (3); This rotary kiln pyrogenation chamber is tilted to down layout, mixed gas outlet after being respectively equipped with the import of pyrolysis material feed, heat carrier import, pyrolysis on the rotary kiln pyrogenation chamber and solid product outlet; The import of described pyrolysis material feed is connected with described pyrolysis material charging gear (14); The heat carrier import is connected with the bottom of first cyclone separator; Mixed gas outlet after the pyrolysis links to each other with the inlet of second cyclone separator (7) through pipeline, and the solid product outlet is connected with the emulsion zone of fluidized bed combustion chamber (1) through heat-resisting auger (15).
2. according to the described a kind of organic solid waste pyrolysis gasifying device of claim 1, it is characterized in that: the centre of gyration axis of described rotary kiln pyrogenation chamber and the angle of horizontal plane are 3 °～5 °.
3. according to the described a kind of organic solid waste pyrolysis gasifying device of claim 1, it is characterized in that: described air preheater (8) adopts heat pipe preheater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202636102U CN202203950U (en) | 2011-07-25 | 2011-07-25 | Organic solid waste pyrolyzation and gasification device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202636102U CN202203950U (en) | 2011-07-25 | 2011-07-25 | Organic solid waste pyrolyzation and gasification device |
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| CN202203950U true CN202203950U (en) | 2012-04-25 |
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| CN2011202636102U Expired - Fee Related CN202203950U (en) | 2011-07-25 | 2011-07-25 | Organic solid waste pyrolyzation and gasification device |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102878566A (en) * | 2012-10-12 | 2013-01-16 | 大连理工大学 | Organic solid fuel drying, pyrolyzing and incinerating integrated method and organic solid fuel drying, pyrolyzing and incinerating integrated device |
| CN103148513A (en) * | 2013-03-07 | 2013-06-12 | 华北电力大学（保定） | Biomass pyrolysis double fluidized bed ignition system and working method thereof |
| CN104748125A (en) * | 2015-03-16 | 2015-07-01 | 同济大学 | Pyrolysis volatile matter combustion system |
| CN106753505A (en) * | 2017-01-18 | 2017-05-31 | 武汉大学 | A kind of tilting biomass through pyrolysis reaction unit |
| WO2018044251A1 (en) * | 2016-08-29 | 2018-03-08 | Strizhak Sergii Yu | Method of conversion of municipal solid waste and other carbon-containing feedstock with high content of tars into synthesis gas and the equipment used in this method |
| CN109163330A (en) * | 2018-10-10 | 2019-01-08 | 永清环保股份有限公司 | A kind of domestic garbage pyrolysis gasification process system, processing method and electricity generation system |
| CN109563991A (en) * | 2016-07-28 | 2019-04-02 | 弗罗拉德瑞有限公司 | Fractional combustion |
| CN110172357A (en) * | 2019-06-01 | 2019-08-27 | 中国烟草总公司郑州烟草研究院 | A kind of two-part series connection biomass continuous pyrolysis carbonizing apparatus |
| CN112126472A (en) * | 2020-08-19 | 2020-12-25 | 青岛洪润林业生物质能源有限公司 | Biomass pyrolysis gasification rotary furnace equipment |
-
2011
- 2011-07-25 CN CN2011202636102U patent/CN202203950U/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102878566A (en) * | 2012-10-12 | 2013-01-16 | 大连理工大学 | Organic solid fuel drying, pyrolyzing and incinerating integrated method and organic solid fuel drying, pyrolyzing and incinerating integrated device |
| CN103148513A (en) * | 2013-03-07 | 2013-06-12 | 华北电力大学（保定） | Biomass pyrolysis double fluidized bed ignition system and working method thereof |
| CN104748125A (en) * | 2015-03-16 | 2015-07-01 | 同济大学 | Pyrolysis volatile matter combustion system |
| CN109563991A (en) * | 2016-07-28 | 2019-04-02 | 弗罗拉德瑞有限公司 | Fractional combustion |
| WO2018044251A1 (en) * | 2016-08-29 | 2018-03-08 | Strizhak Sergii Yu | Method of conversion of municipal solid waste and other carbon-containing feedstock with high content of tars into synthesis gas and the equipment used in this method |
| CN106753505A (en) * | 2017-01-18 | 2017-05-31 | 武汉大学 | A kind of tilting biomass through pyrolysis reaction unit |
| CN109163330A (en) * | 2018-10-10 | 2019-01-08 | 永清环保股份有限公司 | A kind of domestic garbage pyrolysis gasification process system, processing method and electricity generation system |
| CN110172357A (en) * | 2019-06-01 | 2019-08-27 | 中国烟草总公司郑州烟草研究院 | A kind of two-part series connection biomass continuous pyrolysis carbonizing apparatus |
| CN112126472A (en) * | 2020-08-19 | 2020-12-25 | 青岛洪润林业生物质能源有限公司 | Biomass pyrolysis gasification rotary furnace equipment |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120425 Termination date: 20160725 |