CN102329651A - Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification - Google Patents
Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification Download PDFInfo
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Abstract
The invention provides a three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification. The three-stage gasification device is provided with a reacting furnace as a main body, the reacting furnace is in a cylindrical or square structure, an upper pyrolysis hearth inside the reacting furnace is a biomass pyrolysis reaction chamber, a lower gasification hearth is a pyrolysis product steam fluidization and gasification chamber, and a middle hearth of the reacting furnace is provided with an annular catalyst bed layer (a catalytic pyrolysis and gasification chamber). The upper pyrolysis hearth is provided with a feeding device and communicated with the lower gasification hearth. The bottom of the lower gasification hearth is provided with a mixed gas inlet. The upper end of the furnace body of the reaching furnace is provided with a smoke outlet connected with a cyclone separator. A temperature control device is respectively and correspondingly arranged at the outer side of the reacting furnace. An experiment system for the whole production process of synthesis gas is simplified, the gas yield of a gasification furnace is increased, the quality of the synthesis gas is improved, and the tar content in the produced gas is reduced. The device provided by the invention has the advantages of convenience in temperature control, energy saving, environment friendliness, continuation in running, simple structure and the like.
Description
Technical field
The invention belongs to the biomass energy chemical technology field, particularly a kind of three-section type biomass pyrolytic gasification is produced the gasification installation of synthetic gas.
Technical background
Biomass are the various organisms that form through photosynthesis; It derives from the photosynthesis of green plants directly or indirectly, can be converted into conventional solid-state, liquid state and gaseous fuel, and its distributes extensively, amount usable is big; It is a kind of renewable energy source; And also be unique a kind of reproducible contain hydrocarbon component and heat energy, storable natural raw material, utilize biomass to carry out energy utilization and Chemical Manufacture, have CO
2The characteristic of zero release.Along with the minimizing day by day of traditional fossil energy reserves, and because the problem of environmental pollution that uses fossil energy to bring, pay attention to and develop common recognition renewable, that eco-friendly power source has become national governments.Through methods such as thermochemistry, biological chemistries; Can biomass be changed into the gas or the liquid fuel of cleaning; Produce combined diesel oil/gasoline, Chemicals and satisfy electricity needs or the like, have the potentiality that comprehensively substitute fossil energy, become the new forms of energy that first develop countries in the world.
The method that biomass is changed into clean air or liquid fuel is a lot, and wherein, biomass thermal chemical conversion technology can adapt to all biomass kinds with other compared with techniques, and has the ability that large industrialized is produced, and is easy to mass-producing and uses.Biomass pyrogenation gasification prepares synthetic gas, and (staple is H
2With CO gas); And then synthetic liquid fuel (like methyl alcohol, ethanol, dme, alkene, diesel oil and petroleum naphtha etc.) is one of biomass energy recycling approach that has most in the thermochemistry transformation technology development prospect; Domestic industry circle and the unprecedented attention of academia have been received; And dropped into great amount of manpower and carried out relevant research and development with material resources, wherein through utilizing biomass materials such as stalk, rice husk, firewood to obtain extensive studies through the technology that the preparation of elevated temperature heat chemical process contains the synthetic gas of hydrogen and carbon monoxide.Biomass pyrogenation gasification prepares that gasifying reactor is its nucleus equipment in the synthesis gas process.The processing parameter of the form of gasifying reactor, structure, operation has direct influence to the quality of product synthetic gas.Therefore; Exploitation efficient biomass pyrolysis gasifying device is produced high-quality synthetic gas; And be converted into fuel such as liquefied hydrocarbon, alcohols and ethers through follow-up synthesis reactor; Both can alleviate dependence, also can reduce the consumption of domestic traditional fossil energy, have the social benefit of active protection environment simultaneously international crude oil market.
The gasifying reactor (vapourizing furnace) that is used for gasifying biomass at present roughly can be divided into three kinds: fixed bed, air flow bed and fluidized-bed.Fixed-bed gasification furnace simple in structure, easy to operate, operator scheme is flexible, but non-uniform temperature heat exchange effect is relatively poor in the stove, contains a large amount of tar in the outlet synthetic gas.The operating temperature of air flow bed is higher; Temperature is more even in the stove; Tar cracking degree in air flow bed is higher; But entrained flow gasification is had relatively high expectations to the solid material particle diameter, and the raw material that gets into air flow bed need be worn into very tiny particle, and this has proposed the another one technical barrier for the grinding of the biomass material that contains a large amount of fibers.And fluidized bed gasification reactor can be handled the high-moisture material because thermal capacity is high, adaptability to raw material is strong.In addition, it also has higher heat transfer and rate of mass transfer.Fluidized-bed endogenous substance particle can fully contact with the bed material, be heated evenly, in gasifying reactor, be the Boiling Combustion state, gasification reaction speed is fast, gasification efficiency is high, temperature is high and stable in the gasifying reactor; Be suitable for continuous large-scale production, therefore enjoy attention.But it is very sensitive that fluidized-bed reactor also exists the physical property of raw material, operates waywardly, and operating temperature is general also lower, and the coal-tar middle oil content of outlet synthetic gas is also considerable, and CH in the aerogenesis
4And CO
2Content is higher, generally needs follow-up equipment to handle problems such as tar and reformation synthetic gas, makes gasification system and the device more complicated that becomes.
To improve the concentration of synthetic gas in the aerogenesis, reduce CH in the aerogenesis through the staging treating biomass material
4And CO
2Content and reduction tar content are to solve fluidized-bed reactor to prepare one of method of high-quality synthetic gas requirement.Biomass solid at first prepares the coke (semicoke) and the cracked gas of biomass high yield through thermo-cracking under this lower temperature in 300～600 ℃ of left and right sides; The coke (semicoke) that then pyrolysis is produced is sent to and carries out high temperature (700～900 ℃) gasification reaction with water vapor in the fluidized bed gasification reactor and prepare crude synthesis gas, and the tar of complete reaction and the crude synthesis gas that makes do not pass through catalytic pyrolysis (reformation) bed again and further issue the quality that green coke oil breaking and crude synthesis gas reforming reaction improve synthetic gas in the effect of catalyzer.
Is biomass the secondhand energy of cleaning through pyrolysis, gasification, catalytic pyrolysis/reformation segmentation reaction conversion; Can obtain dual effective effect; The one, can solve problem of environmental pollution; The 2nd, can reduce dependence to the oil coal resources, for build a resource-conserving society with friendly environment society play active effect.
Summary of the invention
The object of the invention proposes the gasification installation that a kind of simple, efficient, energy-conservation three-section type biomass pyrolytic gasification is produced synthetic gas being to overcome the defective that existing biomass prepare the synthetic gas technology.
The present invention realizes through following technical proposals:
Main body of the present invention is a Reaktionsofen, adopts cylindrical or square structure, and its inner epimere pyrolysis burner hearth form biomass pyrolysis reaction chamber is a purpose to produce coke mainly; The hypomere gasification hearth is the water vapor fluidized gasification chamber of pyrolysis product, and the water vapor gasification reaction of coke (semicoke) mainly takes place, and generates high-quality synthetic gas; And the middle part burner hearth of Reaktionsofen is provided with cyclic beds (catalytic pyrolysis/reforming reaction chamber), and the gas reforming reaction of the catalytic pyrolysis and the crude synthesis gas of a small amount of tar mainly takes place, and to improve the ratio of synthesis gas in the aerogenesis, reduces tar, methane and CO
2Content.Said epimere pyrolysis burner hearth is provided with feeding unit, and epimere pyrolysis burner hearth is communicated with the hypomere gasification hearth.Hypomere gasification hearth bottom is provided with mixed gas inlet.Reaktionsofen body of heater upper end is provided with the flue gas air outlet, and the flue gas air outlet is connected with cyclonic separator.The Reaktionsofen outside and epimere pyrolysis burner hearth, hypomere gasification hearth, the corresponding temperature regulating device that is respectively arranged with of beds.
The feeding unit that said epimere pyrolysis burner hearth is provided with can be: the biomass hopper is communicated with feeding screw; Feeding screw is communicated with epimere pyrolysis burner hearth through the hypomere tremie pipe; And the side at tremie pipe is provided with the nitrogen inlet pipe, guarantees that biomass material can drop in the biomass pyrolytic chamber under the effect of nitrogen gas stream smoothly.Screw feeding device outer setting has water cooling plant simultaneously, and pyrolytic reaction takes place to guarantee biomass material in fill process, can not be heated in advance, thereby guarantees the unobstructed of biomass material charging.
Described epimere pyrolysis burner hearth interlude can be provided with the conical pipeline section of a convergent, and the angle that forms with the upper end tube wall is 45 °, falls smoothly in pyrolytic process to guarantee biomass material.
Described hypomere gasification hearth lower end can be provided with a conical gas spreading area; And be provided with porous ceramic tile distributor in the middle of hypomere gasification hearth and the conical gas spreading area; The conical gas spreading area is to come in order to guarantee can evenly spread along the taper spreading area from the high-temperature gas mixture that the preheating gas inlet mouth gets into; Porous ceramic tile distributor is in order to make the high-temperature gas mixture body that gets into body of heater can uniform distribution, thus guarantee reaction mass and fluidizing medium can be under the effect of air-flow even fluidisation.Bottom, conical gas spreading area communicates with the mixed gas preheating chamber; The mixed gas preheating chamber communicates with mixed gas inlet; Mixed gas preheating chamber outer setting has temperature control unit; Through controlled temperature is set, to air and the water vapor mixing preheating that feeds, to guarantee that later stage water vapor gasification reaction carries out smoothly.
Can be placed with the fixedly screen cloth of coke tar cracking and crude synthesis gas catalytic reforming catalyst in the described beds, to guarantee that catalyzer can stably be positioned in the fixed bed in reaction process.Said catalyzer can be a kind of also possibly be multiple catalyst mixture.The preferred nickel-containing catalyst that uses in the beds.
The biomass pyrolytic reaction chamber of apparatus of the present invention, water vapor fluidized gasification chamber, catalytic pyrolysis/reforming reaction chamber are arranged in the same body of heater; But three sections body of heater sides all are equipped with TP and temperature control unit; In reaction process; Can be through the temperature that the differential responses section is set carry out temperature control to each section respectively, guarantee in the reaction process pyrolysis, gasification and catalytic pyrolysis/reforming process is relatively independent and carry out continuously.
The present invention compares with the device that other biological matter prepares synthetic gas, has the following advantages and beneficial effect:
The present invention combines the pyrolysis characteristics of biomass, the gasification property of biomass coke (semicoke), the catalytic pyrolysis of tar and the CR characteristic of crude synthesis gas; Catalytic pyrolysis (reformation) process that biomass pyrogenation gasification is prepared pyrolysis section, gasification section, tar and crude synthesis gas in the synthetic gas process is separated; Make each step of reaction different stove sections in same device relatively separately and carry out continuously simplify the experimental system that biomass prepare synthetic gas.Biomass reduce tar content significantly through high-temperature water vapor gasification, catalytic cracking of tar and the crude synthesis gas reforming reaction of low temperature pyrogenation, coke (semicoke), reduce methane and CO in the aerogenesis
2Content produces the high-quality synthetic gas that is applicable to the synthetic prepare liquid fuel of Fischer-Tropsch, reaches clean and effective and utilizes this renewable energy source of biomass energy.The present invention is simple, efficient, energy-conservation, economy and Project Realization property are strong, improved significantly gasification system gasification efficiency, reduced effective synthetic gas oxygen-consumption, improved the energy transformation ratio of total system and guaranteed stability of system etc.
Apparatus of the present invention have convenient temperature control, energy-conserving and environment-protective, and operation is continuous, advantages of simple structure and simple, high-quality synthetic gas is produced in biological material pyrolysis such as stalk capable of using, rice husk, sawdust.
Description of drawings
Fig. 1 is an apparatus structure synoptic diagram of the present invention.
Description of reference numerals: 1, biomass silo, 2, feeding screw, 3, the tremie pipe of feeder, 4, epimere pyrolysis burner hearth, 5, beds; 6, hypomere gasification hearth, 7, porous ceramic tile distributor, 8, the conical gas spreading area, 9, the preheating gas inlet mouth; 10, gas mixture (air and water vapor) preheating chamber, 11, mixed gas inlet, 12, exhanst gas outlet, 13, temperature control unit; 14, temperature control unit, 15, temperature control unit, 16, smoke separator (cyclonic separator), 17, go out ash bucket.
The practical implementation method
As shown in Figure 1; Novel three-stage pyrolytic gasification of the present invention prepares the device of synthetic gas; Comprise Reaktionsofen, the tubular furnace lining of Reaktionsofen is processed by silicon carbide material or corundum material, and Reaktionsofen comprises the inboard ring-type beds [5] in epimere pyrolysis burner hearth [4], hypomere gasification hearth [6] and stage casing.Be provided with the screw feeding device on epimere pyrolysis burner hearth [4] top; The screw feeding device comprises the tremie pipe [3] of biomass hopper [1], feeding screw [2] and feeder; The tremie pipe of feed-pipe [3] is inserted in the epimere pyrolysis burner hearth [4] of pyrolysis gasifying device, and tremie pipe [3] is provided with nitrogen inlet.Epimere pyrolysis burner hearth [4] interlude is provided with the conical pipeline section of a convergent, and the angle that forms with the upper end tube wall is 45 °, falls smoothly in pyrolytic process to guarantee biomass material.The bottom of epimere pyrolysis burner hearth [4] is connected with hypomere gasification hearth [6]; Gasification hearth [6] bottom is provided with a conical gas spreading area [8]; Be provided with the porous ceramic tile distributor [3] of percentage of open area between 10～30% in the middle of gasification hearth [6] and conical gas spreading area [8]; Bottom, conical gas spreading area [8] is preheating gas inlet mouth [9], and preheating gas inlet mouth [9] is connected with mixed gas preheater [10], and mixed gas preheater [10] bottom is provided with a mixed gas inlet [11].Inboard, pyrolytic gasification reaction unit body of heater stage casing is provided with the catalyst fixed bed layer of ring-type [5]; Right side, body of heater upper end is provided with flue gas air outlet [12]; Flue gas air outlet [12] is connected with cyclonic separator [16], and cyclonic separator top is provided with the fume emission mouth, and the bottom is provided with out ash bucket [17].The pyrolysis gasifying device outside is respectively arranged with three sections temperature regulating devices [13], [14] and [15].
During this device operation; By feeding screw [2] tremie pipe [3] of the biomass in the biomass silo [1] via its lower end joined in the epimere pyrolysis burner hearth [4]; Under the control of temperature control unit [13], carry out the low temperature pyrogenation reaction, the product of biomass low temperature pyrogenation is mainly biomass coke (semicoke) and cracked gas.Under the effect of nitrogen gas stream; Pyrolysis product constantly come downwards in the hypomere gasification hearth [6] with mixed gas preheater [10] in the water vapor mixture body generation high-temperature water vapor gasification reaction of coming in; Gasification temperature is controlled through temperature control unit [15]; The mixed gas charge flow rate is controlled through mass flowmeter, makes interior pyrolysis coke (semicoke) of stove and fluidizing medium be in fluidized state, and gasification reaction is fully carried out; And the preheating gas that gas preheater [10] is come in carries out cloth wind through porous ceramic tile distributor [7], and the mixing preheating gas that makes into can uniform distribution.In this process, main pyrolysis product coke (semicoke) further generates crude synthesis gas with water vapor generation water-gas reaction.A small amount of tar that then produces behind the pyrolytic gasification and the crude synthesis gas that makes are again via the inboard ring-type beds [5] of stove; Under the effect of nickel-base catalyst and through temperature control unit [14], carry out temperature control; Thereby the water vapour catforming reaction of catalytic cracking of tar and crude synthesis gas takes place, and generation does not contain tar or tar content high-quality synthesis gas seldom.The gas-entrained that produces the not a small amount of coke and the biomass lime-ash of complete reaction gets in the cyclonic separator [16] through exhanst gas outlet [12] together; Pass through cyclonic separation; The gas that produces is separated with the participation lime-ash; The gas of generation is purified, and lime-ash is collected in out in the ash bucket [17] and carries out other application.
The above is merely preferred embodiment of the present invention, is not the present invention is done any pro forma restriction; The those of ordinary skill of all industry all can be by the above with shown in the Figure of description and embodiment of the present invention swimmingly; In every case the change of making not breaking away from technical scheme of the present invention, the equivalent variations of modifying and developing are equivalent embodiment of the present invention, all still belong to the protection domain of technical scheme of the present invention.
Claims (6)
1. a three-section type biomass pyrolytic gasification prepares the device of synthetic gas; Comprise Reaktionsofen; It is characterized in that: the inner epimere pyrolysis of Reaktionsofen burner hearth form biomass pyrolysis reaction chamber; The hypomere gasification hearth is the water vapor fluidized gasification chamber of pyrolysis product, and the middle part burner hearth of Reaktionsofen is provided with the cyclic beds; Said epimere pyrolysis burner hearth is provided with feeding unit, and epimere pyrolysis burner hearth is communicated with the hypomere gasification hearth, and hypomere gasification hearth bottom is provided with mixed gas inlet; Reaktionsofen body of heater upper end is provided with the flue gas air outlet, and the flue gas air outlet is connected with cyclonic separator; The Reaktionsofen outside and epimere pyrolysis burner hearth, hypomere gasification hearth, the corresponding temperature regulating device that is respectively arranged with of beds.
2. three-section type biomass pyrolytic gasification as claimed in claim 1 prepares the device of synthetic gas; It is characterized in that the feeding unit that said epimere pyrolysis burner hearth is provided with is: the biomass hopper is communicated with feeding screw; Feeding screw is communicated with epimere pyrolysis burner hearth through the hypomere tremie pipe, and is provided with the nitrogen inlet pipe in a side of tremie pipe; Screw feeding device outer setting has water cooling plant simultaneously.
3. three-section type biomass pyrolytic gasification as claimed in claim 1 prepares the device of synthetic gas; It is characterized in that described epimere pyrolysis burner hearth interlude is provided with the conical pipeline section of a convergent; The angle that forms with the upper end tube wall is 45 °, falls smoothly in pyrolytic process to guarantee biomass material.
4. three-section type biomass pyrolytic gasification as claimed in claim 1 prepares the device of synthetic gas; It is characterized in that: described hypomere gasification hearth lower end can be provided with a conical gas spreading area; And be provided with porous ceramic tile distributor in the middle of hypomere gasification hearth and the conical gas spreading area; Bottom, conical gas spreading area communicates with the mixed gas preheating chamber, and the mixed gas preheating chamber communicates with mixed gas inlet, and mixed gas preheating chamber outer setting has temperature control unit.
5. three-section type biomass pyrolytic gasification as claimed in claim 1 prepares the device of synthetic gas, it is characterized in that: be placed with the fixedly screen cloth of coke tar cracking and crude synthesis gas catalytic reforming catalyst in the described beds.
6. prepare the device of synthetic gas like claim 1 or 5 described three-section type biomass pyrolytic gasifications, it is characterized in that: use nickel-containing catalyst in the beds.
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| CN105925321A (en) * | 2016-07-12 | 2016-09-07 | 安徽省化工设计院 | Dedusting and decoking integrated biomass gasifier |
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2055503U (en) * | 1989-07-08 | 1990-04-04 | 清华大学 | Single-stage fluidized bed powder coal gasified furnace |
| US4968325A (en) * | 1987-08-24 | 1990-11-06 | Centre Quebecois De Valorisation De La Biomasse | Fluidized bed gasifier |
| CN2461925Y (en) * | 2001-02-13 | 2001-11-28 | 王同章 | Circulating fluidized bed gasification furnace |
| JP2004182903A (en) * | 2002-12-04 | 2004-07-02 | Kawasaki Heavy Ind Ltd | Method and apparatus for gasifying biomass |
| CN2677376Y (en) * | 2004-01-16 | 2005-02-09 | 中国科学院广州能源研究所 | Down-draft gasification furnace |
| JP2006265454A (en) * | 2005-03-25 | 2006-10-05 | Ngk Insulators Ltd | Circulating fluidized gasification furnace |
| CN101245264A (en) * | 2008-03-25 | 2008-08-20 | 东南大学 | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method |
| CN101407724A (en) * | 2008-10-27 | 2009-04-15 | 合肥天焱绿色能源开发有限公司 | Vertical combined gasification furnace for solid biomass |
| CN101747943A (en) * | 2008-12-01 | 2010-06-23 | 中国农业科学院农业环境与可持续发展研究所 | Method by utilizing livestock manure to produce hydrogenous gas and other products in a step-by-step thermal decomposition way and device |
| CN102021038A (en) * | 2009-09-14 | 2011-04-20 | 新奥科技发展有限公司 | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification |
-
2011
- 2011-08-26 CN CN201110249081.5A patent/CN102329651B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968325A (en) * | 1987-08-24 | 1990-11-06 | Centre Quebecois De Valorisation De La Biomasse | Fluidized bed gasifier |
| CN2055503U (en) * | 1989-07-08 | 1990-04-04 | 清华大学 | Single-stage fluidized bed powder coal gasified furnace |
| CN2461925Y (en) * | 2001-02-13 | 2001-11-28 | 王同章 | Circulating fluidized bed gasification furnace |
| JP2004182903A (en) * | 2002-12-04 | 2004-07-02 | Kawasaki Heavy Ind Ltd | Method and apparatus for gasifying biomass |
| CN2677376Y (en) * | 2004-01-16 | 2005-02-09 | 中国科学院广州能源研究所 | Down-draft gasification furnace |
| JP2006265454A (en) * | 2005-03-25 | 2006-10-05 | Ngk Insulators Ltd | Circulating fluidized gasification furnace |
| CN101245264A (en) * | 2008-03-25 | 2008-08-20 | 东南大学 | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method |
| CN101407724A (en) * | 2008-10-27 | 2009-04-15 | 合肥天焱绿色能源开发有限公司 | Vertical combined gasification furnace for solid biomass |
| CN101747943A (en) * | 2008-12-01 | 2010-06-23 | 中国农业科学院农业环境与可持续发展研究所 | Method by utilizing livestock manure to produce hydrogenous gas and other products in a step-by-step thermal decomposition way and device |
| CN102021038A (en) * | 2009-09-14 | 2011-04-20 | 新奥科技发展有限公司 | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification |
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