CN203112765U - Tree-reactor biomass pyrolysis system - Google Patents
Tree-reactor biomass pyrolysis system Download PDFInfo
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- CN203112765U CN203112765U CN 201320107945 CN201320107945U CN203112765U CN 203112765 U CN203112765 U CN 203112765U CN 201320107945 CN201320107945 CN 201320107945 CN 201320107945 U CN201320107945 U CN 201320107945U CN 203112765 U CN203112765 U CN 203112765U
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- fluidized bed
- calcinator
- outlet
- rotary type
- reactor
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Abstract
The utility model belongs to the technical field of novel biomass pyrolysis systems, and particularly relates to a three-reactor biomass pyrolysis system and an operating method thereof. The system comprises a quick fluidized bed oxidation oven, a first cyclone separator, a smoke pipeline, a first material return valve, a bubbling fluidized bed calcinator, a second material return valve, a second cyclone separator, a CO2 pipeline, a third material return valve, a rotary type pyrolysis furnace, a feeding port, a fuel gas outlet and a hot auger. According to the system, the three-reactor design structure of the quick fluidized bed oxidation oven, the bubbling fluidized bed calcinator and the rotary type pyrolysis furnace are adopted, working condition parameters such as the reaction temperature of each reactor are independent and associated with one another, and main influence factor is a relationship between the selection and the proportioning of materials with double chemical chains; according to the system and the method, zero emission of the CO2 is changed into negative emission; and H2 component content in the fuel gas is greater than 80%, so that the heat loss of the biomass energy is reduced, pollution hazard to the environment caused by semi-coke is prevented.
Description
Technical field
The utility model belongs to novel biomass pyrolysis system technical field, particularly a kind of three reactor organisms matter pyrolysis systems.
Background technology
In the fossil energy of various countries, the world today day by day under the exhausted background, biomass energy as a kind of safe and reliable, standing stock are big, environmentally friendly and reproducible energy form, more and more are subjected to various countries researchist's attention.In recent years, the development of the biomass energy utilization technologies of China is swift and violent, and by the end of the year 2010, China's biomass power generation installation total amount has surpassed 2000 MW.
Gasifying biomass, pyrolysis are applied widely as utilize the technique means of biomass energy on a large scale 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 the biomass pyrolysis process, directly be discharged in the environment with slag, this way had both caused the loss of energy, again environment had been caused pollution.
(3) there is not the decarburization link, a large amount of CO in the Wood Adhesives from Biomass process usually
2Just directly be discharged in the 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.
The utility model content
At the prior art deficiency, the utility model provides a kind of three reactor organisms matter pyrolysis systems.
A kind of three reactor organisms matter pyrolysis systems, the top outlet of its fast fluidized bed oxidized still is connected with first cyclonic separator; The top of described 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 links to each other with the bottom of fast fluidized bed oxidized still by the second returning charge valve; The top exit of bubbling fluidization bed calcinator links to each other with second cyclonic separator; CO is passed through at the top of described second cyclonic separator
2Pipeline and CO
2Capturing device links to each other, 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 links to each other with hot auger inlet end; Hot auger exit end links to each other with the bottom of bubbling fluidization bed calcinator.
The beneficial effects of the utility model are:
(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 the 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 the harm of semicoke pollution on the environment simultaneously.
Description of drawings
Fig. 1 is the utility model system and device structural representation;
Number in the figure: 1-fast fluidized bed oxidized still; 2-first cyclonic separator; The 3-flue; The 4-first returning charge valve; 5-bubbling fluidization bed calcinator; The 6-second returning charge valve; 7-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 utility model provides a kind of three reactor organisms matter pyrolysis systems, below in conjunction with the drawings and specific embodiments the utility model is described further.
A kind of three reactor organisms matter pyrolysis systems, the top outlet of its fast fluidized bed oxidized still 1 is connected with first cyclonic separator 2; The top of described 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 links to each other 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 links to each other with second cyclonic separator 7; CO is passed through at the top of described second cyclonic separator 7
2Pipeline 8 and CO
2Capturing device links to each other, 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 links to each other with hot auger 13 inlet ends; Hot auger 13 exit end link to each other 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 the 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 the bubbling fluidization bed calcinator 5
3CaO and CO that calcining and decomposing produces
2Enter into second cyclonic separator 7 with fluidized, CaO and CO under action of gravity
2Gas solid separation comes, and CaO enters in the rotary type pyrolysis oven 10 by the 3rd returning charge valve 9, CO
2Pass through CO
2Pipeline 8 enters into CO
2In the capturing device, so far finish the circulation of one of them chain in two chemical chain reaction;
The circulation process of another one chemistry 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 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 takes place 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 that when moisture participated in, this reacted easier carrying out, and has therefore fed 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 control of reaction in furnace temperature is about 650 ℃, and the required heat of reaction in the vapourizing furnace comes from the physics sensible heat of CaO.
2, bubbling fluidization bed calcinator
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 the CO of generation and H with the water vapour that adds
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 taken place in CO.These three kinds of reactions are thermopositive reaction, though the reaction need the heating.Temperature of reaction is about 800 ℃.
（7）
In the 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 about 800 ℃.
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 finishing the total system flow process.This reaction is oxidizing reaction fast, emits a large amount of heat, and temperature is about 850 ℃.
Claims (1)
1. reactor organisms matter pyrolysis system is characterized in that: the top outlet of fast fluidized bed oxidized still (1) is connected with first cyclonic separator (2); The top of described 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) links to each other 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) links to each other with second cyclonic separator (7); CO is passed through at the top of described second cyclonic separator (7)
2Pipeline (8) and CO
2Capturing device links to each other, 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 links to each other with hot auger (13) inlet end; Hot auger (13) exit end links to each other with the bottom of bubbling fluidization bed calcinator (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320107945 CN203112765U (en) | 2013-03-07 | 2013-03-07 | Tree-reactor biomass pyrolysis system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320107945 CN203112765U (en) | 2013-03-07 | 2013-03-07 | Tree-reactor biomass pyrolysis system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203112765U true CN203112765U (en) | 2013-08-07 |
Family
ID=48893133
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201320107945 Expired - Fee Related CN203112765U (en) | 2013-03-07 | 2013-03-07 | Tree-reactor biomass pyrolysis system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203112765U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103113919A (en) * | 2013-03-07 | 2013-05-22 | 华北电力大学（保定） | Biomass pyrolysis system of three-stage reactor and working method thereof |
| CN104061568A (en) * | 2014-06-26 | 2014-09-24 | 东南大学 | Method and device for capturing CO2 through Cu/Ca-based compound combined cycle |
| CN108730964A (en) * | 2018-06-15 | 2018-11-02 | 华北电力大学（保定） | One kind of multiple solid fuel chemistry chain combustion apparatus and method |
-
2013
- 2013-03-07 CN CN 201320107945 patent/CN203112765U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103113919A (en) * | 2013-03-07 | 2013-05-22 | 华北电力大学（保定） | Biomass pyrolysis system of three-stage reactor and working method thereof |
| CN104061568A (en) * | 2014-06-26 | 2014-09-24 | 东南大学 | Method and device for capturing CO2 through Cu/Ca-based compound combined cycle |
| CN108730964A (en) * | 2018-06-15 | 2018-11-02 | 华北电力大学（保定） | One kind of multiple solid fuel chemistry chain combustion apparatus and method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130807 Termination date: 20140307 |