CN103113919A - Biomass pyrolysis system of three-stage reactor and working method thereof - Google Patents
Biomass pyrolysis system of three-stage reactor and working method thereof Download PDFInfo
- Publication number
- CN103113919A CN103113919A CN2013100756048A CN201310075604A CN103113919A CN 103113919 A CN103113919 A CN 103113919A CN 2013100756048 A CN2013100756048 A CN 2013100756048A CN 201310075604 A CN201310075604 A CN 201310075604A CN 103113919 A CN103113919 A CN 103113919A
- Authority
- CN
- China
- Prior art keywords
- charge valve
- returning charge
- fluidized bed
- reaction
- enters
- 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.)
- Pending
Links
Images
Classifications
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention belongs to the technical field of a novel biomass pyrolysis system, and particularly relates to a biomass pyrolysis system of a three-stage reactor and a working method thereof. The system disclosed by the invention is composed of a rapid fluidized bed oxidization furnace, a first cyclone separator, a flue gas duct, a first return valve, a bubbling fluidized bed calcining furnace, a second return valve, a second cyclone separator, a CO2 pipeline, a third return valve, a rotary pyrolyzing furnace, a feeding hole, a gas outlet and a hot packing auger. The design structure of the three-stage reactor of the rapid fluidized bed oxidization furnace, the bubbling fluidized bed calcining furnace and the rotary pyrolyzing furnace is adopted; the work condition parameters such as reaction temperature of each reactor have independent and associated relation; and the main influencing factor is material selection and matching relationship of double chemical chains. The CO2 is converted into negative discharge from zero discharge; the content of the H2 component in the gas is greater than 80%; the heat loss of biomass energy is reduced; and meanwhile, pollution hazard on the environment caused by semicoke is prevented.
Description
Technical field
The invention belongs to novel biomass pyrolysis system technical field, particularly a kind of three reactor organisms matter pyrolysis system and method for works thereof.
Background technology
In the fossil energy of world day by day under exhausted background, biomass energy as a kind of safe and reliable, standing stock are large, environmentally friendly and reproducible energy form, more and more are subject to various countries researchist's attention.In recent years, the development of the biomass energy utilization technologies of China is swift and violent, ends for the end of the year 2010, and China's biomass power generation installation total amount has surpassed 2000 MW.
Gasifying biomass, pyrolysis are applied widely as utilize on a large scale the technique means of biomass energy in industrial production.And there is following problem in present geseous fuel that solid biomass is converted into:
(1) combustion gas of gasifying biomass generation has mixed a large amount of N
2, CO
2With foreign gases such as water vapour, cause the calorific value of combustion gas lower.
(2) produce a large amount of semicokes in biomass pyrolysis process, directly be discharged in environment with slag, this way had both caused the loss of energy, again environment had been caused pollution.
(3) usually there is no the decarburization link, a large amount of CO in the Wood Adhesives from Biomass process
2Just directly be discharged in atmosphere without any processing, the Greenhouse effect of initiation are more and more serious, and are inconsistent with current low-carbon (LC) production operation mode.
Summary of the invention
Not enough for prior art, the invention provides a kind of three reactor organisms matter pyrolysis system and method for works thereof.
A kind of three reactor organisms matter pyrolysis systems, the top outlet of its fast fluidized bed oxidized still is connected with the first cyclonic separator; The top of described the first cyclonic separator arranges flue, and outlet at bottom is connected with the upper entrance of bubbling fluidization bed calcinator by the first returning charge valve; The lower part outlet of described bubbling fluidization bed calcinator is connected with the bottom of fast fluidized bed oxidized still by the second returning charge valve; The top exit of bubbling fluidization bed calcinator is connected with the second cyclonic separator; CO is passed through at the top of described the second cyclonic separator
2Pipeline and CO
2Capturing device is connected, and outlet at bottom is connected with the rotary type pyrolysis oven by the 3rd returning charge valve; Described rotary type pyrolysis oven top arranges material inlet and gas outlet, and lower part outlet is connected with hot auger inlet end; Hot auger exit end is connected with the bottom of bubbling fluidization bed calcinator.
A kind of method of work of three reactor organisms matter pyrolysis systems, its concrete scheme is as follows:
Water vapour enters system from the second returning charge valve, the first returning charge valve, bubbling fluidization bed calcinator and the 3rd returning charge valve respectively; Air enters in the middle of system bottom the fast fluidized bed oxidized still;
Biomass material enters into the rotary type pyrolysis oven by material inlet, after air generating gasification pyrolytic reaction, generation contain semicoke carbon granules and CO
2Preliminary combustion gas aerogenesis with react from the CaO of the 3rd returning charge valve, generate and be used for industrial combustion gas, the CaCO that reaction produces
3Enter into the bubbling fluidization bed calcinator with the semicoke carbon granules via hot auger and carry out high-temperature calcination decomposition and reduction CuO reaction, wherein semicoke carbon granules and water vapour react, the H that produces
2, CO together with unreacted semicoke carbon granules with carry out redox reaction from the first returning charge valve with from the CuO of fast fluidized bed oxidized still, and heat release makes CaCO
3Decompose; CaCO in the bubbling fluidization bed calcinator
3CaO and CO that calcining and decomposing produces
2Enter into the second cyclonic separator with fluidized, CaO and CO under action of gravity
2Gas solid separation comes, and CaO enters in the rotary type pyrolysis oven by the 3rd returning charge valve, CO
2Pass through CO
2Pipeline enters into CO
2In capturing device, so far complete the circulation of one of them chain in two chemical chain reaction;
The circulation process of another one chemical chain is: air and Cu from blower fan together enter from the bottom of fast fluidized bed oxidized still, and carry out oxidizing reaction fast, the CuO that generates enters the first cyclonic separator with hot waste gas under fluidized state, CuO enters into the bubbling fluidization bed calcinator by action of gravity through the first returning charge valve and participates in redox reaction.
Beneficial effect of the present invention is:
(1) when carrying out suitability for industrialized production, paid attention to the high concentration CO that system is produced
2Capture control, CO
2Transfer negative emission to by zero release, the CO of incinerator outlet
2Concentration is greater than 85%;
(2) by biomass pyrolytic and carry out the combustion gas decarburization, H in combustion gas
2Component concentration is greater than 80%; Combustion gas unit's calorific value is greatly improved, and has had more usury value;
(3) semicoke that produces of biomass pyrolytic gasifies in calcination reactor, has reduced the thermosteresis of biomass energy, has prevented simultaneously the harm of semicoke pollution on the environment.
Description of drawings
Fig. 1 is system and device structural representation of the present invention;
Number in the figure: 1-fast fluidized bed oxidized still; 2-the first cyclonic separator; The 3-flue; 4-the first returning charge valve; 5-bubbling fluidization bed calcinator; 6-the second returning charge valve; 7-the second cyclonic separator; 8-CO
2Pipeline; 9-the 3rd returning charge valve; 10-rotary type pyrolysis oven; The 11-material inlet; The 12-gas outlet; The hot auger of 13-.
Embodiment
The invention provides a kind of three reactor organisms matter pyrolysis system and method for works thereof, the present invention will be further described below in conjunction with the drawings and specific embodiments.
A kind of three reactor organisms matter pyrolysis systems, the top outlet of its fast fluidized bed oxidized still 1 is connected with the first cyclonic separator 2; The top of described the first cyclonic separator 2 arranges flue 3, and outlet at bottom is connected with the upper entrance of bubbling fluidization bed calcinator 5 by the first returning charge valve 4; The lower part outlet of described bubbling fluidization bed calcinator 5 is connected with the bottom of fast fluidized bed oxidized still 1 by the second returning charge valve 6; The top exit of bubbling fluidization bed calcinator 5 is connected with the second cyclonic separator 7; CO is passed through at the top of described the second cyclonic separator 7
2Pipeline 8 and CO
2Capturing device is connected, and outlet at bottom is connected with rotary type pyrolysis oven 10 by the 3rd returning charge valve 9; Described rotary type pyrolysis oven 10 tops arrange material inlet 11 and gas outlet 12, and lower part outlet is connected with hot auger 13 inlet ends; Hot auger 13 exit end are connected with the bottom of bubbling fluidization bed calcinator 5.
A kind of method of work of three reactor organisms matter pyrolysis systems, its concrete scheme is as follows:
Water vapour enters system from the second returning charge valve 6, the first returning charge valve 4, bubbling fluidization bed calcinator 5 and the 3rd returning charge valve 9 respectively; Air enters in the middle of system by fast fluidized bed oxidized still 1 bottom;
Biomass material enters into rotary type pyrolysis oven 10 by material inlet 11, after air generating gasification pyrolytic reaction, generation contain semicoke carbon granules and CO
2Preliminary combustion gas aerogenesis with react from the CaO of the 3rd returning charge valve 9, generate and be used for industrial combustion gas, the CaCO that reaction produces
3Enter into bubbling fluidization bed calcinator 5 with the semicoke carbon granules via hot auger 13 and carry out high-temperature calcination decomposition and reduction CuO reaction, wherein semicoke carbon granules and water vapour react, the H that produces
2, CO together with unreacted semicoke carbon granules with carry out redox reaction from the first returning charge valve 4 with from the CuO of fast fluidized bed oxidized still 1, and heat release makes CaCO
3Decompose; CaCO in bubbling fluidization bed calcinator 5
3CaO and CO that calcining and decomposing produces
2Enter into the second cyclonic separator 7 with fluidized, CaO and CO under action of gravity
2Gas solid separation comes, and CaO enters in rotary type pyrolysis oven 10 by the 3rd returning charge valve 9, CO
2Pass through CO
2Pipeline 8 enters into CO
2In capturing device, so far complete the circulation of one of them chain in two chemical chain reaction;
The circulation process of another one chemical chain is: air and Cu from blower fan together enter from the bottom of fast fluidized bed oxidized still 1, and carry out oxidizing reaction fast, the CuO that generates enters the first cyclonic separator 2 with hot waste gas under fluidized state, CuO enters into bubbling fluidization bed calcinator 5 by action of gravity through the first returning charge valve 4 and participates in redox reactions.
Adopt two chemical chain reaction, concrete response situation is as follows:
1, rotary type pyrolysis oven
[C
xH
yO
z]→tar1+char1→
tar2[CH
0.85O
0.17]+char2[CH
0.20O
0.13]
+H
2+CO+CO
2+CH
4+C
2H
4+ （1）
This reaction is with C
xH
yO
zFor pyrolytic reaction occurs in the biomass material of main body composition in the rotary type pyrolysis oven, generate the preliminary splitting gas that is become to be grouped into by multiple gases, wherein comprised a large amount of CO
2, caused the unstable of burning, be unsuitable for direct burn application.Endothermic heat of reaction ,+1000 kJ/kg.
This reaction is for adding CaO, with the CO of absorption cracking generation in biomass material
2Research thinks, when having moisture to participate in, this reaction is more easily carried out, so has passed into the suitable quantity of water steam in the 4th returning charge valve.Endothermic heat of reaction (temperature is unsuitable too high) ,+175.7 kJ/mol.
The reaction in furnace temperature is controlled at 650 ℃ of left and right, and the required heat of reaction in vapourizing furnace comes from the physics sensible heat of CaO.
2, bubbling fluidization bed calcinator
（3）
Failing the carbon granules (semicoke) of complete reaction in the rotary type pyrolysis oven enters in the bubbling fluidization bed calcinator of high temperature and reacts with the water vapour that adds, the CO of generation and H
2Be mainly used to reduce CuO but not go to carry out burn application as combustion gas.Reaction will absorb a large amount of heat ,+131.5 kJ/mol.
2CuO+C→2Cu+CO
2 （4）
CuO+H
2→Cu+H
2O （5）
CuO+CO→Cu+CO
2 （6）
High temperature CuO and three kinds of typical reductive agent C, H from the fast fluidized bed oxidized still
2, redox reaction occured in CO.These three kinds of reactions are thermopositive reaction, although the reaction need the heating.Temperature of reaction is 800 ℃ of left and right.
（7）
In bubbling fluidization bed calcinator under fluidized state, CaCO
3The CaO that thermolysis produces is with CO
2Enter cyclonic separator, enter in the rotary type pyrolysis oven after the CaO solid materials is separated, be rich in CO
2Gas collect.Endothermic heat of reaction, temperature of reaction are 800 ℃ of left and right.
3, fast fluidized bed oxidized still
2Cu+O
2→2CuO （8）
The chemical chain reaction of carrying out in the fast fluidized bed oxidized still is mainly this a pair of chemical chain reaction process oxidation material CuO is provided, as a kind of intermediate medium of completing the whole system flow process.This reaction is oxidizing reaction fast, emits a large amount of heat, and temperature is 850 ℃ of left and right.
Claims (2)
1. reactor organisms matter pyrolysis system is characterized in that: the top outlet of fast fluidized bed oxidized still (1) is connected with the first cyclonic separator (2); The top of described the first cyclonic separator (2) arranges flue (3), and outlet at bottom is connected with the upper entrance of bubbling fluidization bed calcinator (5) by the first returning charge valve (4); The lower part outlet of described bubbling fluidization bed calcinator (5) is connected with the bottom of fast fluidized bed oxidized still (1) by the second returning charge valve (6); The top exit of bubbling fluidization bed calcinator (5) is connected with the second cyclonic separator (7); CO is passed through at the top of described the second cyclonic separator (7)
2Pipeline (8) and CO
2Capturing device is connected, and outlet at bottom is connected with rotary type pyrolysis oven (10) by the 3rd returning charge valve (9); Described rotary type pyrolysis oven (10) top arranges material inlet (11) and gas outlet (12), and lower part outlet is connected with hot auger (13) inlet end; Hot auger (13) exit end is connected with the bottom of bubbling fluidization bed calcinator (5).
2. the method for work of three reactor organisms matter pyrolysis systems as claimed in claim 1, is characterized in that, concrete scheme is as follows:
Water vapour enters system from the second returning charge valve (6), the first returning charge valve (4), bubbling fluidization bed calcinator (5) and the 3rd returning charge valve (9) respectively; Air enters in the middle of system bottom fast fluidized bed oxidized still (1);
Biomass material enters into rotary type pyrolysis oven (10) by material inlet (11), after air generating gasification pyrolytic reaction, generation contain semicoke carbon granules and CO
2Preliminary combustion gas aerogenesis with react from the CaO of the 3rd returning charge valve (9), generate and be used for industrial combustion gas, the CaCO that reaction produces
3Enter into bubbling fluidization bed calcinator (5) with the semicoke carbon granules via hot auger (13) and carry out high-temperature calcination decomposition and reduction CuO reaction, wherein semicoke carbon granules and water vapour react, the H that produces
2, CO together with unreacted semicoke carbon granules with carry out redox reaction from the first returning charge valve (4) with from the CuO of fast fluidized bed oxidized still (1), and heat release makes CaCO
3Decompose; CaCO in bubbling fluidization bed calcinator (5)
3CaO and CO that calcining and decomposing produces
2Enter into the second cyclonic separator (7) with fluidized, CaO and CO under action of gravity
2Gas solid separation comes, and CaO enters in rotary type pyrolysis oven (10) by the 3rd returning charge valve (9), CO
2Pass through CO
2Pipeline (8) enters into CO
2In capturing device, so far complete the circulation of one of them chain in two chemical chain reaction;
The circulation process of another one chemical chain is: air and Cu from blower fan together enter from the bottom of fast fluidized bed oxidized still (1), and carry out oxidizing reaction fast, the CuO that generates enters the first cyclonic separator (2) with hot waste gas under fluidized state, CuO enters into bubbling fluidization bed calcinator (5) by action of gravity through the first returning charge valve (4) and participates in redox reaction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100756048A CN103113919A (en) | 2013-03-07 | 2013-03-07 | Biomass pyrolysis system of three-stage reactor and working method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100756048A CN103113919A (en) | 2013-03-07 | 2013-03-07 | Biomass pyrolysis system of three-stage reactor and working method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103113919A true CN103113919A (en) | 2013-05-22 |
Family
ID=48412338
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013100756048A Pending CN103113919A (en) | 2013-03-07 | 2013-03-07 | Biomass pyrolysis system of three-stage reactor and working method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103113919A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104099111A (en) * | 2014-07-21 | 2014-10-15 | 武汉海德新能源投资有限公司 | Continuous and overall biomass pyrolysis furnace |
| WO2019137056A1 (en) * | 2018-01-09 | 2019-07-18 | 华南理工大学 | Oxygen carrier/carbon carrier-based biomass chemical looping gasification method and device |
| 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 |
| WO2023152464A1 (en) * | 2022-02-11 | 2023-08-17 | Wild Hydrogen Limited | Method and apparatus for gasification of biogenic material |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040060237A1 (en) * | 2001-07-31 | 2004-04-01 | General Electric Company | Process for converting coal into fuel cell quality hydrogen and sequestration-ready carbon dioxide |
| CN1544309A (en) * | 2003-11-12 | 2004-11-10 | 浙江大学 | Oxygen needless hydrogen making method from solid fuel without waste gas discharging |
| CN1795257A (en) * | 2003-05-29 | 2006-06-28 | 阿尔斯托姆科技有限公司 | Hot solids gasifier with co sb 2 /sb removal and hydrogen production |
| CN101333463A (en) * | 2008-08-04 | 2008-12-31 | 上海发电设备成套设计研究院 | Oxygen supplying and hydrogen making process from iron base oxygen carrier of three-linked transport bed |
| CN101539037A (en) * | 2009-04-03 | 2009-09-23 | 东南大学 | Method for catching carbon dioxide by pressurized fluidized bed combustion combined recycle generating system |
| WO2010043799A2 (en) * | 2008-10-17 | 2010-04-22 | Jean-Xavier Morin | Method and device for extracting carbon dioxide from the atmosphere |
| CN102200277A (en) * | 2011-04-27 | 2011-09-28 | 东南大学 | Chemical chain combustion method and device through solid fuel |
| CN102655928A (en) * | 2009-09-16 | 2012-09-05 | 西班牙高等科研理事会 | Method for recovering CO2 by means of CaO and the exothermic reduction of a solid |
| CN202546743U (en) * | 2012-03-23 | 2012-11-21 | 华北电力大学 | Solid fuel chemical looping combustion system based on three-bed-structured fuel reactor |
| CN203112765U (en) * | 2013-03-07 | 2013-08-07 | 华北电力大学（保定） | Tree-reactor biomass pyrolysis system |
-
2013
- 2013-03-07 CN CN2013100756048A patent/CN103113919A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040060237A1 (en) * | 2001-07-31 | 2004-04-01 | General Electric Company | Process for converting coal into fuel cell quality hydrogen and sequestration-ready carbon dioxide |
| CN1795257A (en) * | 2003-05-29 | 2006-06-28 | 阿尔斯托姆科技有限公司 | Hot solids gasifier with co sb 2 /sb removal and hydrogen production |
| CN1544309A (en) * | 2003-11-12 | 2004-11-10 | 浙江大学 | Oxygen needless hydrogen making method from solid fuel without waste gas discharging |
| CN101333463A (en) * | 2008-08-04 | 2008-12-31 | 上海发电设备成套设计研究院 | Oxygen supplying and hydrogen making process from iron base oxygen carrier of three-linked transport bed |
| WO2010043799A2 (en) * | 2008-10-17 | 2010-04-22 | Jean-Xavier Morin | Method and device for extracting carbon dioxide from the atmosphere |
| WO2010043799A3 (en) * | 2008-10-17 | 2010-11-25 | Jean-Xavier Morin | Method for the pyrolysis and gasification of biomasses by means of thermochemical conversion |
| CN101539037A (en) * | 2009-04-03 | 2009-09-23 | 东南大学 | Method for catching carbon dioxide by pressurized fluidized bed combustion combined recycle generating system |
| CN102655928A (en) * | 2009-09-16 | 2012-09-05 | 西班牙高等科研理事会 | Method for recovering CO2 by means of CaO and the exothermic reduction of a solid |
| CN102200277A (en) * | 2011-04-27 | 2011-09-28 | 东南大学 | Chemical chain combustion method and device through solid fuel |
| CN202546743U (en) * | 2012-03-23 | 2012-11-21 | 华北电力大学 | Solid fuel chemical looping combustion system based on three-bed-structured fuel reactor |
| CN203112765U (en) * | 2013-03-07 | 2013-08-07 | 华北电力大学（保定） | Tree-reactor biomass pyrolysis system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104099111A (en) * | 2014-07-21 | 2014-10-15 | 武汉海德新能源投资有限公司 | Continuous and overall biomass pyrolysis furnace |
| WO2019137056A1 (en) * | 2018-01-09 | 2019-07-18 | 华南理工大学 | Oxygen carrier/carbon carrier-based biomass chemical looping gasification method and device |
| 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 |
| WO2023152464A1 (en) * | 2022-02-11 | 2023-08-17 | Wild Hydrogen Limited | Method and apparatus for gasification of biogenic material |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103062910B (en) | Method and device for integrating chemical-looping combustion with CO<2> trapping | |
| CN100582197C (en) | Circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method | |
| CN103740389B (en) | The multi-production process of low-rank coal cascade utilization | |
| CN102746903B (en) | Large-scale domestic garbage dry distillation and gasification furnace without exhaust gas or dioxin emission | |
| CN103934254B (en) | A kind of system and method for cement kiln associated treatment domestic waste | |
| CN103756731B (en) | A kind of reciprocating cycle double fluidized bed solid fuel gasification device and method | |
| CN102925219B (en) | Device for resource utilization of circulating fluidized bed coal-gasified discharged ash and use method | |
| CN103528067B (en) | Domestic garbage pyrolysis and low heat value pyrolysis gas combustion integrative technique | |
| CN202203950U (en) | Organic solid waste pyrolyzation and gasification device | |
| CN104629809B (en) | The system that high heating value biomass gasified gas are produced with oxygen-enriched combustion boiler high-temperature flue gas | |
| CN112029518A (en) | System and method for preparing activated carbon by integrating carbonization and activation of coal/biomass | |
| Lu et al. | Nitrogen evolution during the co-combustion of hydrothermally treated municipal solid waste and coal in a bubbling fluidized bed | |
| CN103113919A (en) | Biomass pyrolysis system of three-stage reactor and working method thereof | |
| CN110564452A (en) | Biomass double fluidized bed catalytic gasification combined cycle power generation method and system with copper slag as circulating bed material | |
| CN203112765U (en) | Tree-reactor biomass pyrolysis system | |
| CN102589147B (en) | Method for combusting solid fuel by chemical looping and device thereof | |
| CN215048660U (en) | Solar heat supply chemical chain air separation oxygen generation system and comprehensive energy utilization system thereof | |
| CN204267081U (en) | A kind of coal mine gas low emission catalytic oxidation heating system | |
| CN203605233U (en) | Household garbage thermolysis and low-heating-value thermolysis gas combustion integrated device | |
| CN202494117U (en) | Paratactic type half gasification household garbage digestion furnace | |
| CN101581451B (en) | Heat processing technology and heat processing device for realizing near-zero discharge of domestic garbage | |
| CN214307052U (en) | Low-nitrogen biomass gas combustion and activated carbon activation system | |
| CN202101422U (en) | Device performing chemical-looping combustion by utilizing solid fuels | |
| CN108592016B (en) | Low NOx emission circulating fluidized bed boiler for burning high-nitrogen biomass | |
| CN108680017B (en) | Reheat furnace system and furnace apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20130522 |