CN102191089A - Two-stage high-temperature preheated steam biomass gasification furnace - Google Patents
Two-stage high-temperature preheated steam biomass gasification furnace Download PDFInfo
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- CN102191089A CN102191089A CN2011100767594A CN201110076759A CN102191089A CN 102191089 A CN102191089 A CN 102191089A CN 2011100767594 A CN2011100767594 A CN 2011100767594A CN 201110076759 A CN201110076759 A CN 201110076759A CN 102191089 A CN102191089 A CN 102191089A
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- 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
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Abstract
The invention discloses a two-stage high-temperature preheated steam biomass gasification furnace. According to the invention, steam with a high temperature is used as a gasification agent. Fuel gas with high quality and high heat value is obtained through the gasification of the biomass. Meanwhile, active carbon, which is a byproduct, is produced. The gasification furnace is composed by a first reactor and a second reactor. The first reactor is a fixed bed gasification section, where volatile matters in feedings are removed. During the process, only high-temperature preheated pure steam provided by a high-temperature air generator is used. The second reactor is a spouted bed gasification section, where a high-temperature preheated mixture of air and steam is used for a complete cracking reaction and a tar breaking reaction. The biomass gasification furnace provided by the present invention has advantages of high gasification efficiency, high gasification speed, complete reaction, high utilance of raw materials, and is energy saving and environment protecting. The fuel gas produced by the gasification furnace has advantages of good quality and high heat value.
Description
Technical field
The present invention relates to the gasifying biomass field, be specially a kind of two-part high temperature preheating steam biomass gasifying furnace that can carry out two-part ultrahigh-temperature gasification operation biomass.
Background technology
Biomass high-temperature air gasification technology is a new and high technology in fuel utilization and the power supply field; to alleviating energy crisis with to improve environmental quality significant; be subjected to the great attention of academia and industry member in some developed countries such as Japan, the U.S., West Europe; China's research work in this respect is at the early-stage; high temperature air gasification process itself is lacked enough research, go back the more perfect experimental system that can be used for high temperature air gasification research of none at present.
Summary of the invention
Technical problem solved by the invention is to provide a kind of two-part high temperature preheating steam biomass gasifying furnace, to solve the shortcoming in the above-mentioned background technology.
Technical problem solved by the invention realizes by the following technical solutions:
Two-part high temperature preheating steam biomass gasifying furnace is divided into two-stage reactor, sloughs the volatile matter in the feed in first step reactor.The pure steam of the high temperature preheating that in this process, only utilizes High-temperature Air Generator to provide (700 ℃-1000 ℃).In the reactor of the second stage, utilize the air and the steam mixture (temperature is at 700 ℃-1400 ℃) of high temperature preheating to carry out the reaction of abundant cracking and destruction tar.
In the present invention, high-temperature steam and air mixture are mainly provided by High-temperature Air Generator in the vapourizing furnace.
In the present invention, the vapourizing furnace body of heater is the pass column structure, inside is divided into two-stage reactor, two-layer reactor is a cucurbit formula structure, the inclination angle of the other furnace wall of the side of its contraction place is between 45-60 °, narrower place, centre separates by fire grate, in addition, also be provided with a fire grate under the reactor of the second stage of bottom, this fire grate structure is slag trapping chamber down, under described two fire grate structures, all be provided with spout, be respectively top and bump mouth and bottom spout, two spouts are cylindricality passageway structure, the other gas inlet that all has of side, the gas inlet of its middle and upper part is the high-temperature steam inlet, and the gas inlet of bottom is high-temperature steam and gas inlet.
In addition, corresponding charging and discharging port should be set also on vapourizing furnace, preferred version is: in the first step reactor upper end solid feed import that a vertical direction feeds should be set, and the side side also should be provided with an artificial fuel gas outlet; Other liquid and the particulate feed injection port of being provided with of second stage reactor-side; Simultaneously, slag trapping chamber is provided with a slag-drip opening.
In the present invention, the optional material of solid feed can be biomass, coal, municipal solid refuse and composition thereof.
In first step reactor, the material of giving be higher than 700 ℃ high-temperature steam sensible heat by vapor temperature, and the obvious heat of smoke heating that in the reactor of the second stage, produces by the oxidation of charcoal ash, gasification.
The high-temperature steam that is used for the gasification of first step reactor feed is sent into by the high-temperature steam inlet, and enters the top spout; At this moment, must keep high-temperature steam to supply with continuously,, be preferably more than 700 ℃ so that first step reactor temperature remains on 600 ℃-900 ℃ in the high-temperature steam ingress.
In this process, because the gaseous combustion that remaining oxygen and material pyrolytic decomposition discharge flame may occur near the fire grate of top.
By control vapor temperature, the flow velocity sent into from the high-temperature steam ingress, and the temperature of unnecessary oxygen and content are controlled temperature in the first step reactor in the reactor of the second stage in the gasification.The residence time of feed is mainly controlled by the size in fire grate gap, top in the first step reactor.
For vaporized chemical can be mixed well with material, the bottom fire grate is arranged with the bottom spout, the diameter of the spout generally furnace diameter than first step reactor is little, and the diameter of the port section that enters spout of high-temperature steam inlet should be the 1/2-1/3 of top spout.
Fuel is sloughed volatile matter by high-temperature steam in first step reactor after, remain not volatile carbon and form gac and lime-ash.Lime-ash continues to fall, successively by top fire grate, top spout and second stage reactor, and lime-ash and high temperature air, vapour mixture generation oxidation, gasification reaction in this process.Temperature at bottom fire grate place reactor can further be elevated to the degree that is lower than grey softening temperature.High temperature air and steam mixture enter the bottom spout by high-temperature steam and gas inlet.During operation in the reactor of the second stage maximum of temperature should remain below about 50 ℃ of grey softening temperatures, and the temperature when being lower than 100 ℃ of softening temperatures is as the top temperature of works better.
The temperature of second stage reactor is controlled by the ratio of steam and oxygen in preheating temperature, flow velocity, the mixture and the ratio of steam and carbon.
Lime-ash is discharged after falling into bottom slag trapping chamber by the bottom spout in batches.
Artificial fuel gas flows out by the artificial fuel gas outlet.Because the temperature of first step reactor is enough high and have steam to exist, most of tar is destroyed, changes into synthetic gas, thereby the main chemical compositions of synthetic gas is H
2, CO, CH
4And CO
2
By optimizing the ratio of input quantity of steam and amount of oxygen, this gasifier can be controlled hydrogen and the ratio of carbon monoxide in synthetic gas well.In addition, the temperature interior by temperature (as being controlled at 700 ℃) in the reactor of the control second stage and first step reactor is identical, can consume all tar and oil.
The present invention also can be used to produce gac, and as long as well-designed process parameter (ratio of temperature, reaction times, oxygen amount and quantity of steam etc.) just can make the output of the product (gac and synthetic gas) of expection reach maximum value.
Main chemical reactions in the first step gasifier:
In first step reactor, the energy that is used to slough volatile matter is provided by pure steam sensible heat of high temperature and the hot steam that comes from second stage reactor.Temperature in the first step reactor is controlled at more than 600 ℃ by the flow and the temperature of the pure steam of high temperature,
In this stage reactor, high-temperature steam mixes with feed (biomass and solid waste), and biomass are heated by high-temperature steam, and the gasification of generation mainly contains:
Simultaneously, because the existence of steam, following reaction takes place in steam and volatile matter,
CO+H
2O→CO
2+H
2 (3)
Volatile matter reacts once more with the minor amounts of oxygen that is discharged by pyrolytic decomposition and second stage reactor:
C
mH
n+(m/2+n/4)O
2→m?CO+n/2H
2O (4)
CO+1/2O
2→CO
2 (5)
H
2+1/2O
2→H
2O (6)
CO+H
2O→CO
2+H
2 (7)
In this process, because first step reactor temperature more than at least 600 ℃ and will control the residence time of feed in this stage reactor, makes gas in this stage reactor be in extremely under the anaerobic environment.Solid, liquid and delay charcoal ash are fallen into second stage reactor under the effect of gravity.
Main chemical reactions in the gasifier of the second stage:
At second stage reactor, the energy that is used for the conversion of charcoal ash heat is provided by the heat that steam, air mixture sensible heat and charcoal ash partial oxidation are generated, and temperature is higher than ash fusion point in the reactor of the second stage, thereby lime-ash flows into soot collector with liquid form.Usually for trees biolobic material feed, second stage temperature of reactor should be 1300 ℃.
When not having other feed (as liquid and particulate) to inject second stage reactor, the principal reaction in the gasifier is (heat equation):
Gasification reaction:
C+O
2*CO
2-393.5KJ/mol (8)
C+H
2O*CO+H
2+1313KJ/mol (9)
C+H
2O*CO
2+H
2+90.2KJ/mol (10)
The particulate oxide reaction:
C+1/2O
2*CO-110.5KJ/mol (11)
The Bu Duoaer reaction:
C+CO
2*2CO-172.4KJ/mol (12)
Water-gas shift reaction:
CO+H
2O*CO
2+H
2-41.1KJ/mol (13)
Methanation reaction:
CO+3H
2*CH
4+H
2O-206.1KJ/mol?(14)
Hydrogenation:
C+2H
2*CH
4-75KJ/mol (15)
When other feed (liquid and particulate) was sent in the reactor of the second stage, from (1) to (15) all reactions all can take place.
Because many reactions take place simultaneously, accurately control whole process is the comparison difficulty.However, by well-designed process parameter (ratio of temperature, reaction times, oxygen amount and quantity of steam etc.), can make product (gac and the synthetic gas) output of expection reach maximum value.
Generally speaking, in this vapourizing furnace, feed is gasified by the pure steam of high temperature (more than 600 ℃) in first step reactor earlier, and carbon is activated by high-temperature steam in the reactor of the second stage then.
Utilize the present invention to prepare gac:
The preparation of gac was divided into for two steps: in order at utmost to reduce oxygen, protium and under high temperature (500 ℃-1000 ℃) oxygen free condition, carry out the raw material carbonization process and the reactivation process of the carbonated product under oxygenant (water, carbonic acid gas, water and the carbonic acid gas etc.) catalytic condition is arranged at high temperature.
In this vapourizing furnace, two kinds of production process of active carbon are arranged: first method is utilized first step reactor, sends into high-temperature steam by the high-temperature steam inlet, closes the high-temperature steam and the gas inlet that transport high-temperature steam and air mixture; In the second approach, select to allow two reactors work simultaneously, but high-temperature steam and gas inlet are only sent into high-temperature steam, at this moment can directly collect dry activated carbon.
The high-temperature steam of sending into from high-temperature steam and gas inlet in the reactor of the second stage can make the micropore of gac open, thereby second method can be produced high-quality gac.Diameter by the vapor temperature adjustable activity charcoal micropore in the reactor of the control second stage: vapor temperature is high more, and the quantity of micropore is many more on the gac.
Therefore, this vapourizing furnace can be produced two kinds of products (gas mixture and gac) with a kind of feed.Share shared separately in the product decides according to the type of feed and the price of product etc.
Utilize treatment liq of the present invention and particulate feed:
By further discovering, this vapourizing furnace can also be used to handle macromole (diameter is greater than 0.5cm) carbonaceous material or small molecules particulate or liquid feeding.
Liquid with the tangent line of particulate feed is: link to each other with second stage reactor by two spray guns; Liquid feeding (as the residue liquid of collecting from ASR microwave oven thermal degradation process) or particulate feed can both be admitted in the reactor of the second stage.
The feed of sending into tangentially enters second stage reactor, with high temperature air that comes from the top fire grate and vapor mixing.The tangent line injection mode can increase the liquid and the residence time of particulate feed in reactor.The flowing gas of carrying secretly leaves producer gas generator from the artificial fuel gas outlet after entering first step reactor by fixed top fire grate.
In order to increase the feed residence time, liquid and the design of particulate feed injection port are in the lower furnace portion of second stage reactor.In general, to a undersized producer gas generator, the position of injection port should be under the fire grate of bottom the 10cm place.The residence time of feed in reactor is by injection speed and the decision of lance ejection angle.
The institute of gasifier internal label (1)-(15) responds and all can take place at this moment.
Beneficial effect: the present invention can effectively improve fuel gases calorific value, enlarges fuel and utilizes scope, reduces environmental pollution, dwindles size, the reduction purification expense of refining plant, thereby improves the economic benefit of vapourizing furnace, improves gasification efficiency.
Description of drawings
Fig. 1 is a gasification system schema of the present invention;
Fig. 2 is the structural representation of vapourizing furnace of the present invention.
Embodiment
For technique means, creation characteristic that the present invention is realized, reach purpose and effect is easy to understand, below in conjunction with concrete diagram, further set forth the present invention.
In an embodiment, selected material is a solid globules, so the liquid of body of heater bottom and particulate feed injection port 11 are in closing condition.
In the present embodiment, selected solid globules diameter is about 8mm (listing in the parameter of wooden bead such as the table 1), mass rate with 97Kg/h under the effect at gravity of the wooden bead under 15 ℃ of room temperatures is supplied with first step reactor 3 from solid feed feed end 1, pass through top fire grate 8 by first step reactor 3 backs, enter second stage reactor 4 then, again by bottom fire grate 5, discharge at slag-drip opening 14 places into slag up to going in slag trapping chamber 6, whole process is all carried out within columniform furnace wall 2.
In first step reactor 3, feed is the obvious heat of smoke heating that the oxidation of charcoal ash, gasification produce in 900 ℃ high-temperature steam sensible heat and the second stage reactor 4 by temperature.The high-temperature steam that is used for the gasification of first step reactor 3 feeds is sent into top spout 13 by high-temperature steam inlet 7; High-temperature steam 7 places that enter the mouth send into, and keep in the first step reactor 3 temperature at 900 ℃.
The technical parameter of wooden bead among table one: the embodiment one
In first step reactor 3, feed is the obvious heat of smoke heating that the oxidation of charcoal ash, gasification produce in 900 ℃ high-temperature steam sensible heat and the second stage reactor 4 by temperature.The high-temperature steam that is used for the gasification of first step reactor 3 feeds is sent into top spout 13 by high-temperature steam inlet 7; High-temperature steam 7 places that enter the mouth send into, and keep in the first step reactor 3 temperature at 900 ℃.
Material is sloughed volatile matter by high-temperature steam in first step reactor 3 after, remain not volatile carbon and form gac and lime-ash.Lime-ash continues to fall, successively by top fire grate 8, top spout 13 and second stage reactor 4, and lime-ash and high temperature air, vapour mixture generation oxidation, gasification reaction in this process.Temperature at fire grate 5 place's reactors can further be elevated to the degree that is lower than grey softening temperature.High temperature air and steam mixture enter bottom spout 10 by high-temperature steam and gas inlet 9.During operation in the second stage reactor 4 maximum of temperature remain below about 50 ℃ of grey softening temperatures.
Simultaneously, high-temperature preheated air and steam mixture are with 90Nm
3The volumetric flow rate of/h is fed in the vapourizing furnace by high-temperature steam and gas inlet 9, and the temperature of preheated mixture is 1332 ℃, and the concentration of oxygen is 9% (volume fraction) in the mixture, and the concentration of steam is 51% in the mixture.High temperature air and vapour mixture meet with the wooden bead that comes from solid feed entrance end 1 then through second reactor 4 and first reactor 3.
Gasification product (being synthetic gas) exports 12 from artificial fuel gas and flows out.The temperature that artificial fuel gas exports the synthetic gas at 12 places is 554 ℃.The low heat value of the synthetic gas that generates is 8.1MJ/Nm
3H in the synthetic gas that generates
2, CO and CH
4Concentration (volume fraction under the drying regime) be respectively 16.4%, 25.1%, 4.3%.
More than show and described ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; that describes in the foregoing description and the specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.The claimed scope of the present invention is defined by appending claims and equivalent thereof.
Claims (3)
1. two-part high temperature preheating steam biomass gasifying furnace, it is characterized in that, the vapourizing furnace body of heater is the pass column structure, inside is divided into two-stage reactor, two-layer reactor is a cucurbit formula structure, the inclination angle of the other furnace wall of the side of its contraction place is between 45-60 °, and narrower place, centre separates by fire grate, in addition, under the reactor of the second stage of bottom, also be provided with a fire grate, this fire grate structure for slag trapping chamber, under described two fire grate structures, all is provided with spout down, spout is a cylindricality passageway structure, the other gas inlet that has of spout side, the gas inlet of its middle and upper part is the high-temperature steam inlet, the gas inlet of bottom is high-temperature steam and gas inlet; Simultaneously, corresponding charging and discharging port should be set also on vapourizing furnace, be specially: in the first step reactor upper end solid feed import that a vertical direction feeds should be set, and the side side also should be provided with an artificial fuel gas outlet; Other liquid and the particulate feed injection port of being provided with of second stage reactor-side; In addition, also be provided with slag-drip opening in the slag trapping chamber.
2. a kind of two-part high temperature preheating steam biomass gasifying furnace according to claim 1 is characterized in that the bottom spout of described second stage reactor, the diameter of the spout generally furnace diameter than first step reactor are little.
3. a kind of two-part high temperature preheating steam biomass gasifying furnace according to claim 1 is characterized in that, the diameter of the port section that enters spout of described high-temperature steam inlet should be the 1/2-1/3 of the diameter of top spout.
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Cited By (16)
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| CN102391893A (en) * | 2011-10-10 | 2012-03-28 | 秦恒飞 | Biomass gasification-activation combination and preparation method of active porous carbon material |
| CN102504878A (en) * | 2011-11-07 | 2012-06-20 | 驻马店市华轩实业有限公司 | Biomass microwave cracking gasification unit |
| WO2013075292A1 (en) * | 2011-11-23 | 2013-05-30 | Ren Jie | Vaporizer for producing combustible gas |
| CN103232862A (en) * | 2013-04-10 | 2013-08-07 | 山西鑫立能源科技有限公司 | Coal gangue pyrolysis gasification device |
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| CN103666570A (en) * | 2012-09-20 | 2014-03-26 | 赵广健 | Self-drying biomass gasification system |
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| CN108728169A (en) * | 2018-08-02 | 2018-11-02 | 廊坊达能新能源技术股份有限公司 | The biomass gasification system of reduced tar content |
| CN108884399A (en) * | 2015-12-28 | 2018-11-23 | 松下靖治 | gasification furnace |
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| CN115353911A (en) * | 2022-07-28 | 2022-11-18 | 中国科学院大学 | Chemical chain gasification hydrogen production and CO production of high-water-content biomass waste 2 Fixing method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2167094Y (en) * | 1993-05-19 | 1994-06-01 | 煤炭科学研究总院北京煤化学研究所 | Water gas generation furnace with up and low blower |
| WO2009145724A2 (en) * | 2008-05-29 | 2009-12-03 | Boson Energy Sa | A two-stage high-temperature preheated steam gasifier |
| CN201678647U (en) * | 2010-04-23 | 2010-12-22 | 中国科学院广州能源研究所 | Step biomass gasification unit |
| CN101982528A (en) * | 2010-11-23 | 2011-03-02 | 神华集团有限责任公司 | Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof |
-
2011
- 2011-03-29 CN CN2011100767594A patent/CN102191089A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2167094Y (en) * | 1993-05-19 | 1994-06-01 | 煤炭科学研究总院北京煤化学研究所 | Water gas generation furnace with up and low blower |
| WO2009145724A2 (en) * | 2008-05-29 | 2009-12-03 | Boson Energy Sa | A two-stage high-temperature preheated steam gasifier |
| CN201678647U (en) * | 2010-04-23 | 2010-12-22 | 中国科学院广州能源研究所 | Step biomass gasification unit |
| CN101982528A (en) * | 2010-11-23 | 2011-03-02 | 神华集团有限责任公司 | Gasification device for classified gasification of moving bed, method for gasifying coal and applications thereof |
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| CN102391893B (en) * | 2011-10-10 | 2013-08-07 | 秦恒飞 | Biomass gasification-activation combination and preparation method of active porous carbon material |
| CN102391893A (en) * | 2011-10-10 | 2012-03-28 | 秦恒飞 | Biomass gasification-activation combination and preparation method of active porous carbon material |
| CN102504878A (en) * | 2011-11-07 | 2012-06-20 | 驻马店市华轩实业有限公司 | Biomass microwave cracking gasification unit |
| WO2013075292A1 (en) * | 2011-11-23 | 2013-05-30 | Ren Jie | Vaporizer for producing combustible gas |
| CN103666570A (en) * | 2012-09-20 | 2014-03-26 | 赵广健 | Self-drying biomass gasification system |
| CN103666569A (en) * | 2012-09-20 | 2014-03-26 | 赵广健 | Biomass gasification system |
| CN103232862B (en) * | 2013-04-10 | 2014-10-08 | 山西鑫立能源科技有限公司 | Coal gangue pyrolysis gasification device |
| CN103232862A (en) * | 2013-04-10 | 2013-08-07 | 山西鑫立能源科技有限公司 | Coal gangue pyrolysis gasification device |
| CN103639172B (en) * | 2013-12-03 | 2017-01-04 | 内蒙古科技大学 | Medical waste high-temperature steam-air gasification sterilization biodegrading process |
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| CN103773505A (en) * | 2014-01-27 | 2014-05-07 | 淄博太沣环保工程有限公司 | Biomass two-stage type gas generating furnace |
| CN108884399A (en) * | 2015-12-28 | 2018-11-23 | 松下靖治 | gasification furnace |
| US11034899B2 (en) | 2015-12-28 | 2021-06-15 | Yasuharu Matsushita | Gasification furnace |
| CN107601427A (en) * | 2017-08-01 | 2018-01-19 | 昆明理工大学 | A kind of biomass gasifying hydrogen making device |
| CN107384485A (en) * | 2017-09-21 | 2017-11-24 | 南京林业大学 | The gas-carbon cogeneration device of ature of coal particle fixed bed gasification |
| CN107384485B (en) * | 2017-09-21 | 2022-12-02 | 南京林业大学 | Gas-carbon co-production device for fixed bed gasification of coal particles |
| CN108728169A (en) * | 2018-08-02 | 2018-11-02 | 廊坊达能新能源技术股份有限公司 | The biomass gasification system of reduced tar content |
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Application publication date: 20110921 |