CN201713504U - Biomass composite gasification device - Google Patents
Biomass composite gasification device Download PDFInfo
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- CN201713504U CN201713504U CN2010202103137U CN201020210313U CN201713504U CN 201713504 U CN201713504 U CN 201713504U CN 2010202103137 U CN2010202103137 U CN 2010202103137U CN 201020210313 U CN201020210313 U CN 201020210313U CN 201713504 U CN201713504 U CN 201713504U
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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
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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
- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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Abstract
The utility model discloses a biomass composite gasification device which comprises a composite gasifier including a gasifier upper flow section, a gasifier transverse flow section and a gasifier lower flow section sequentially communicated inside. The gasifier upper flow section and the gasifier lower flow section are provided with circular sections and the gasifier transverse flow section is provided with a square section; the upper flow section and the lower flow section are connected through the transverse flow section in a tangential manner; a biomass feed opening and a primary gasifying agent inlet are formed on the upper flow section; a secondary gasifying agent inlet is formed on the gasifier transverse flow section; and on the lower flow section, a fuel gas outlet is formed at the lower part and an ash separating area is arranged at the bottom, and an ash outlet is formed in the ash separating area. The device can carry out pyrolysis, gasification, splitting, reforming, and partial oxidation in the same reactor, realizes parameter zone control and optimization, has the advantages of high gasification efficiency, low tar content, strong gas component regulation and control capability, load adaptive capacity and raw material applicability, stable operation and easy amplification, and can be widely applied in fields such as power generation, heating, gas supply, liquid fuel synthesis, etc.
Description
Technical field
The utility model relates to the biomass gasification technology field, especially relates to the biomass combined gasification equipment of removing tar in a kind of stove.
Technical background
Because petroleum resources is day by day deficient, environmental pollution and Greenhouse effect problem serious day by day, obtain higher-grade fuel and chemical becomes a kind of development trend just gradually from abundant biomass agriculture and forestry organic waste material resource (as stalk etc.), at home and abroad cause and show great attention to.Biomass gasification technology can become high-grade geseous fuel with various depleted Wood Adhesives from Biomass, is used for industrial generation, cogeneration, central gas supply, industrial heating heat supply, and provides source of the gas etc. as the synthetic gas synthetic liquid fuel and for fuel cell.Biomass gasification process is because technology is flexible, product is of high grade, characteristics such as of many uses, becomes one of the most promising technology of utilizing in the low-grade biomass.Biomass gasification technology has been subjected to extensive attention both at home and abroad, and correlative study has also obtained significant progress.But still there is bottleneck problem in gasification technology at present, when being particularly useful for low-grade biomass, no matter conventional gasification mode all can't be satisfied the demand from aspects such as tar content, gasification efficiency, gas components, therefore, press for the research gasifying process that tar content is low, combustion gas component ability of regulation and control is strong and easy to operate, solve the bottleneck that exists at present, the biogas metallization processes is made breakthroughs, highlight its superiority in new Application Areas.
At different industrial uses, biomass gasification technology has been carried out a large amount of research and developments both at home and abroad, develop different biogas metallization processes such as fixed bed, fluidized-bed, air flow bed.No matter adopt which kind of gasifying process, the generation of tar is the common problem of gasification technology.Tar is gaseous state when high temperature, mix fully with inflammable gas, and be condensed into liquid state when low temperature, and its separation and processing be difficulty very.The existence of tar has not only reduced gasification efficiency, gas heating value, and more seriously tar is condensed into liquid state when low temperature, and easily and combinations such as water, coke, ash, the obstruction gas pipe line influences the normal operation of equipment for gasification; The tar that is condensed into fine drop is difficult to burn, and is easy to generate particles such as carbon black when burning, and gas-fired equipment is caused great infringement.The existence of tar greatly reduces the utility value of synthetic gas, has stoped the high-end applications of gasification technology, is the bottleneck problem of the efficient large-scale application of gasification technology.
Industrial tar removal method commonly used mainly is that stove is removed outward at present, as dry type filtration, wet scrubbing, catalytic pyrolysis etc.Though filtration and method for washing are simple to operate, cost is lower, efficient is not high, for preventing secondary pollution, need to increase extra treating plant and sewage treatment equipment, not only occupation of land is bigger, has also increased cost of investment, and the tar of disposing can not utilize, and causes the waste of the energy.The catalytic pyrolysis system is simple, capacity usage ratio is high, and the biological fuel gas component is had promotor action and becomes the focus of domestic and international research, but needs to consume a large amount of additional energies, also needs extra utility appliance, has increased the complicacy and the investment of system.Simultaneously,, also do not form business-like special-purpose catalyst series, especially also have bigger distance from commercialization aspect the work-ing life of catalyzer because problems such as catalyst deactivation, mechanical wear and application cost are mainly used in experimental study at present.
Tar also can suppress in vapourizing furnace promptly that tar produces and is target product gas with the tar converted in-situ that produces by the method removed in the stove, realizes not containing tar in the crude synthesis gas in the vapourizing furnace.Remove in the stove and can realize, reduce the purpose that vapourizing furnace exports the coal-tar middle oil content of combustion gas thereby reach by optimizing methods such as adding catalyzer in gasification furnace structure design, optimization gasification operating parameters, the vapourizing furnace.This method is the focus and the Future Development direction of research at present.
Both at home and abroad the development trend of gasification technology be that exploitation is efficient, low tar, gasifying process that combustion gas component ability of regulation and control is stronger.At the effective elimination of tar and the high-end utilization of combustion gas, carried out the research of novel gasifying process both at home and abroad.As: Technical University Of Denmark has designed two-stage gasifier, and the coal-tar middle oil content of gained combustion gas reduces greatly; Germany Choren company has proposed the technology of mild pyrolysis and high temperature pyrolysis two-step method making high quality synthetic gas, contains tar in the synthetic gas hardly.These apparatus features be with many reactors in series on a successive flow process, fuel drying and pyrolysis in the indirect heating type cracker earlier, the cracked product and then lane between cracker and coke gasification device carries out partial oxidation, product gas flow is through the coke bed of heat, thereby makes the coke tar cracking in the product gas and reach lower content.
Therefore, mostly the gasifying process that removes tar at present in the stove is to utilize the series connection of several reactors to realize, having only publication number is that the Chinese patent of " CN101225315A " has proposed incorporate biomass combined gasification equipment, but owing to be subjected to the restriction of structure space, the particle residence time is short, secondary reaction is insufficient in the stove, and the component modulation is indifferent.
Summary of the invention
The utility model provides a kind of biomass combined gasification equipment, can be with reacting phases such as pyrolysis, burning, gasification, coke tar cracking, reformation and component regulation and control to separating, realize the control of parameter subregion and optimize coupling, all processes are finished in a covering device simultaneously, even do not use catalyzer also can reach the purpose that reduces tar content, adjustments of gas component.
For reaching above purpose, the utility model has been taked following technical scheme:
The utility model device comprises composite gasification furnace, and the vapourizing furnace upper flow section that described composite gasification furnace is communicated with successively by inside, vapourizing furnace crossing current section and vapourizing furnace are formed for dirty section.Be provided with biomass feed inlet and a gasification agent inlet in described vapourizing furnace upper flow section; Vapourizing furnace crossing current section is provided with second gasification agent inlet; Described vapourizing furnace upper flow section and dirty section are the circular section, and the crossing current section be the square-section, and upper flow section section tangentially is connected by crossing current with dirty section; The bottom that vapourizing furnace is dirty section is provided with gas outlet, and dirty section bottom of vapourizing furnace is the ash separation district, is provided with the ash content outlet.
Described vapourizing furnace upper flow section can be identical with dirty section diameter, and dirty section height be more than or equal to 2/3 of upper flow section height, and the fluid flow direction in upper flow section and dirty section is opposite, and the ratio of upper flow section sectional area and crossing current section sectional area is greater than 10.
A described gasification agent inlet can be arranged on the bottom of vapourizing furnace upper flow section, makes vaporized chemical enter vapourizing furnace by the bottom of vapourizing furnace upper flow section.
A described vaporized chemical and second gasification agent are air or oxygen or oxygen-rich air, and can add certain water vapour according to reaction needed.The combustion gas that biomass produce at vapourizing furnace upper flow section pyrolytic gasification is carried the tiny solid particle secretly and is tangentially entered dirty section through the crossing current section, because oxidizing reaction takes place in the crossing current section in part combustion gas and second gasification agent, temperature raises rapidly, volume expands rapidly, and the ratio of upper flow section sectional area and crossing current section sectional area is greater than 10, so crossing current section flow velocity can reach more than 10 times of upper flow section flow velocity, when tangentially entering dirty section, combustion gas forms high speed whirlwind, help combustion gas mixing and solid soot particle and separate, prolonged the coke tar cracking of dirty section of vapourizing furnace simultaneously, reform, the secondary reaction time.
Pyrolysis, gasification and biomass coke partial combustion reaction take place in biomass in the vapourizing furnace upper flow section, in vapourizing furnace crossing current section the biological fuel gas partial combustion takes place and react, and in dirty section of vapourizing furnace coke tar cracking, reformation, secondary reaction take place.
In this device, the vapourizing furnace upper flow section is as the biomass pyrogenation gasification district, and temperature is 500-900 ℃, wherein the vapourizing furnace upper flow section in, top form biomass pyrolysis district, temperature is 500-700 ℃, and the bottom of vapourizing furnace upper flow section is biomass coke gasification and partial combustion district, temperature 800-900 ℃; Vapourizing furnace is the high-temperature zone as coke tar cracking, reformation, secondary reaction district for dirty section, and temperature can reach 1000-1300 ℃; The gas outlet pipe of the dirty pars infrasegmentalis gas outlet of vapourizing furnace can stretch into the position of dirty section circular section diameter of about 1/4-1/2 vapourizing furnace in dirty section, prevent to enter the gas outlet pipe along the dirty section isolating solid soot particle of wall backspin, dirty section bottom is the ash separation district, is provided with the ash content outlet.By adding different vaporized chemicals, the temperature of same district not in the control stove, the component of regulating combustion gas realizes the control and the optimization of different operating modes in a stove.
The utility model biomass combined gasification equipment is compound in same reactor with pyrolysis, gasification, cracking, reformation, partial oxidation process, realizes the control of parameter subregion and optimizes.The characteristics that this device has the gasification efficiency height, tar content is low, the gaseous fraction ability of regulation and control is strong, load performance strong, the raw material suitability is strong, stable, be easy to amplify.This device is used for tar content≤20mg/Nm that gasifying biomass can make combustion gas
3, and stable, continuous, can be applicable to multiple field, as generating, heat supply, air feed, synthetic liquid fuel etc.
Description of drawings
Fig. 1 is the utility model device example structure synoptic diagram (front view);
Fig. 2 is the plan structure synoptic diagram of Fig. 1.
Description of reference numerals:
1. 6. gasification agent inlet 7. vapourizing furnaces in dirty section 3. biomass feed inlet of vapourizing furnace upper flow section 2. vapourizing furnaces 4. biomass pyrolytic districts, 5. coke gasifications and partial combustion district crossing current section, 8. second gasification agent, 9. ash separation districts, 10. gas outlets that enter the mouth
Embodiment
Below in conjunction with accompanying drawing and embodiment the utility model content is described further.
As shown in Figure 1, 2, the utility model device comprises composite gasification furnace, and the vapourizing furnace upper flow section 1 that described composite gasification furnace is communicated with successively by inside, vapourizing furnace crossing current section 7 and vapourizing furnace are formed for dirty section 2.Be provided with biomass feed inlet 3 in vapourizing furnace upper flow section 1, the bottom is provided with gasification agent inlet 6 one time; In the vapourizing furnace upper flow section 1, top form biomass pyrolysis district 4, the bottom is coke gasification and partial combustion district 5.The diameter that vapourizing furnace upper flow section 1 and vapourizing furnace are dirty section 2 can be identical, dirty section height is more than or equal to 2/3 of upper flow section height, vapourizing furnace crossing current section 7 is the square-section, the ratio of the sectional area of the sectional area of upper flow section 1 and crossing current section 7 is greater than 10, and the combustion gas that biomass produce at vapourizing furnace upper flow section 1 pyrolytic gasification is carried the tiny solid particle secretly and tangentially entered dirty section 2 of vapourizing furnace through vapourizing furnace crossing current section 7.Be provided with second gasification agent inlet 8 at described vapourizing furnace crossing current section 7 inlets.The bottom that vapourizing furnace is dirty section 2 is provided with gas outlet 10, and the gas outlet pipe stretches into the position of dirty section circular section diameter of about 1/4-1/2 vapourizing furnace in dirty section, and the bottom is ash separation district 9, is provided with the ash content outlet.
Embodiment 1:
Pyrolytic reaction takes place from the pyrolysis zone 4 that opening for feed 3 adds in the composite gasification furnace upper flow section 1 in the biomass wood chip under 500-700 ℃ of temperature, biomass discharge volatilization gas, and generates solid coke; The coke macrobead flows into coke gasification and the partial combustion district 5 in the vapourizing furnace upper flow section 1 downwards, at the oxygen-rich air (O of gasification agent inlet 6 addings
2Concentration 90%) under the effect, small part coke generation oxidizing reaction makes coke gasification and partial combustion district 5 temperature reach 800-900 ℃, and most of coke then generating gasification reaction generates inflammable gas; Upwards provide biomass pyrolytic required heat in mobile high-temperature gas form biomass pyrolysis district 4 from coke gasification and partial combustion district 5, the temperature of keeping pyrolysis zone 4 is at 500-700 ℃; Biomass at gas entrainment tiny solid particle that vapourizing furnace upper flow section 1 internal reaction produces in vapourizing furnace crossing current section 7 tangentially enters dirty section 2 of vapourizing furnace.Add an amount of secondary oxygen-rich air from second gasification agent inlet mouth 8, make part inflammable gas generation oxidizing reaction, temperature raises rapidly, volume expands rapidly, and since the ratio of the sectional area of the sectional area of upper flow section 1 and crossing current section 7 greater than 10, so the flow velocity of crossing current section 7 can reach more than 10 times of flow velocity of upper flow section 1, combustion gas tangentially enters dirty section 2 o'clock formation high speed whirlwind.Dirty section 2 interior local temperature of vapourizing furnace can reach about 1200 ℃, and tar scission reaction takes place under this hot conditions changes into inflammable gas, and the carbon residue in the particle that combustion gas is simultaneously carried secretly also can change into inflammable gas by secondary reaction; Enter in the process of dirty section 2 of vapourizing furnace at the tangential high speed rotating of combustion gas, the solid soot particle that it carries is separated the ash separation district 9 that the bottom of dirty section 2 of downward inflow vapourizing furnace connects from gas under centrifugal action, inflammable gas then enters downstream unit from the gas outlet 10 of dirty section 2 bottom of vapourizing furnace.During oxygen-rich air equivalence ratio ER=0.21-0.29, the gas component that obtains is H
221.4%-25.4%, N
22.9%-3.8%, CO 38.8%-45.2%, CH
44.9%-7.0%, CO
218.5%-25.1%, gasification efficiency 74.9%-85.0%, efficiency of carbon conversion 91.8%-99.6%.Do not feed under the situation of secondary oxygen-rich air vaporized chemical in dirty section 2 of vapourizing furnace, the coal-tar middle oil content of gas outlet 10 inflammable gass can reach 900mg/m
3When feeding secondary oxygen-rich air vaporized chemical, scission reaction takes place in the high-temperature zone in tar, and the tar transformation efficiency can reach 96.8%, and the coal-tar middle oil content of the inflammable gas of gas outlet 10 is reduced to 20mg/m
3Below.Behind the coke tar cracking in the combustion gas each components contents do not have considerable change because coke tar cracking removes N
2Outer other gases all have generation, but coke tar cracking becomes inflammable gas to make the biomass gas generating rate by 1.07Nm
3/ kg brings up to 1.21Nm
3/ kg.
Embodiment 2:
Pyrolytic reaction takes place from the pyrolysis zone 4 that opening for feed 3 adds in the composite gasification furnace upper flow section 1 in the biomass wood chip under 500-700 ℃ of temperature, biomass discharge volatilization gas, and generates solid coke; The coke macrobead flows into coke gasification and the partial combustion district 5 in the vapourizing furnace upper flow section 1 downwards, at the oxygen-rich air (O from gasification agent inlet 6 addings
2Concentration 90%) under the effect, small part coke generation oxidizing reaction makes coke gasification and partial combustion district 5 temperature reach 800-900 ℃, and most of coke then generating gasification reaction generates inflammable gas; Upwards provide biomass pyrolytic required heat in mobile high-temperature gas form biomass pyrolysis district 4 from coke gasification and partial combustion district 5, the temperature of keeping pyrolysis zone 4 is at 500-700 ℃; Biomass at gas entrainment tiny solid particle that vapourizing furnace upper flow section 1 internal reaction produces in vapourizing furnace crossing current section 7 tangentially enters dirty section 2 of vapourizing furnace.Add an amount of secondary oxygen-rich air from second gasification agent inlet mouth 8, make part inflammable gas generation oxidizing reaction, temperature raises rapidly, volume expands rapidly, and since the ratio of the sectional area of the sectional area of upper flow section 1 and crossing current section 7 greater than 10, so the flow velocity of crossing current section 7 can reach more than 10 times of flow velocity of upper flow section 1, combustion gas tangentially enters dirty section 2 o'clock formation high speed whirlwind.For improving H in gas outlet 10 inflammable gass
2/ CO ratio promptly improves H
2Content reduces CO content, improves the synthetic gas quality, adds water vapour in the second gasification agent, by water gas shift reaction CO+H
2O → CO
2+ H
2And steam reforming reaction, gaseous fraction is regulated and control.Local temperature under second gasification agent reaction conditions in dirty section 2 of the vapourizing furnace can reach about 1100 ℃, and tar scission reaction takes place under this hot conditions changes into inflammable gas, and water gas shift reation makes the H in the combustion gas
2Be subjected to directed regulation and control with the CO component; Carbon residue in the particle that combustion gas is simultaneously carried secretly also can change into inflammable gas by secondary reaction; Enter in the process of dirty section 2 of vapourizing furnace at the tangential high speed rotating of combustion gas, the solid soot particle that it carries is separated the ash separation district 9 that the bottom of dirty section 2 of downward inflow vapourizing furnace connects from gas under centrifugal action, inflammable gas then enters downstream unit from the gas outlet 10 of dirty section 2 bottom of vapourizing furnace.Under oxygen-rich air equivalence ratio ER=0.26 situation, when water vapour/biomass material during than (quality) S/B=0.1-0.5, the gas component that obtains is H
224.6%-28.7%, N
22.8%-3.8%, CO 27.1%-33.8%, CH
43.9%-4.1%, CO
229.3%-32.7%, gasification efficiency 73.9%-78%, efficiency of carbon conversion 97.5%-98.4%.With embodiment 1 more as can be known, make H by adding water vapour
2/ CO mean value brings up to 0.88 by 0.56, and the highest having reached more than 1.0 helps follow-up building-up reactions and use, but CO
2Content increases, and needs to remove before synthesizing.
Claims (5)
1. a biomass combined gasification equipment comprises composite gasification furnace, it is characterized in that: the vapourizing furnace upper flow section that described composite gasification furnace is communicated with successively by inside, vapourizing furnace crossing current section and vapourizing furnace are formed for dirty section; Described vapourizing furnace upper flow section and dirty section are the circular section, and the crossing current section be the square-section, and upper flow section section tangentially is connected by crossing current with dirty section; Be provided with biomass feed inlet and a gasification agent inlet in described vapourizing furnace upper flow section; Vapourizing furnace crossing current section is provided with second gasification agent inlet; The bottom that vapourizing furnace is dirty section is provided with gas outlet, and the bottom is the ash separation district, is provided with the ash content outlet.
2. biomass combined gasification equipment as claimed in claim 1, it is characterized in that, described vapourizing furnace upper flow section is as the biomass pyrogenation gasification district, temperature is 500-900 ℃, wherein the vapourizing furnace upper flow section in, top form biomass pyrolysis district, temperature is 500-700 ℃, and the bottom of vapourizing furnace upper flow section is biomass coke gasification and partial combustion district, temperature 800-900 ℃; Dirty section of vapourizing furnace is as coke tar cracking, reformation, secondary reaction district, and temperature can reach 1000-1300 ℃.
3. biomass combined gasification equipment as claimed in claim 1 or 2 is characterized in that, described vapourizing furnace upper flow section is identical with the diameter of dirty section of vapourizing furnace, and dirty section height is more than or equal to 2/3 of upper flow section height; The ratio of described upper flow section sectional area and crossing current section sectional area is greater than 10.
4. biomass combined gasification equipment as claimed in claim 1 is characterized in that, described gas outlet pipe stretches into the position of dirty section circular section diameter of 1/4-1/2 vapourizing furnace in dirty section of the vapourizing furnace.
5. biomass combined gasification equipment as claimed in claim 1 is characterized in that, described second gasification agent inlet is arranged on crossing current section inlet.
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|---|---|---|---|
| CN2010202103137U CN201713504U (en) | 2010-05-24 | 2010-05-24 | Biomass composite gasification device |
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|---|---|---|---|
| CN2010202103137U CN201713504U (en) | 2010-05-24 | 2010-05-24 | Biomass composite gasification device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011147180A1 (en) * | 2010-05-24 | 2011-12-01 | 中国科学院广州能源研究所 | Biomass combined gasification equipment |
| CN103958649A (en) * | 2011-04-06 | 2014-07-30 | 伊内奥斯生物股份公司 | Apparatus and methods for tar removal from syngas |
-
2010
- 2010-05-24 CN CN2010202103137U patent/CN201713504U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011147180A1 (en) * | 2010-05-24 | 2011-12-01 | 中国科学院广州能源研究所 | Biomass combined gasification equipment |
| CN103958649A (en) * | 2011-04-06 | 2014-07-30 | 伊内奥斯生物股份公司 | Apparatus and methods for tar removal from syngas |
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