CN203307297U - Device for preparing low-tar and higher-calorific-value combustible gas by biomass three-phase type gasification - Google Patents
Device for preparing low-tar and higher-calorific-value combustible gas by biomass three-phase type gasification Download PDFInfo
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- CN203307297U CN203307297U CN2013203433392U CN201320343339U CN203307297U CN 203307297 U CN203307297 U CN 203307297U CN 2013203433392 U CN2013203433392 U CN 2013203433392U CN 201320343339 U CN201320343339 U CN 201320343339U CN 203307297 U CN203307297 U CN 203307297U
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Abstract
The utility model discloses a device for preparing low-tar and higher-calorific-value combustible gas by biomass three-phase type gasification. The device is composed of a fluidized bed gasification reactor, a cyclone reforming reactor, a movable bed catalytic reactor and a material returning device, wherein the upper part of the fluidized bed gasification reactor is communicated with the upper part of the cyclone reforming reactor; the lower part of the fluidized bed gasification reactor is communicated with the lower part of the movable bed catalytic reactor through the material returning device; the top of the cyclone reforming reactor is communicated with the top of the movable bed catalytic reactor; a biomass particle charging opening and a first oxygen-enriched/water steam gas inlet are formed in the lower part of the fluidized bed gasification reactor; a second oxygen-enriched/water steam gas inlet is formed in the upper part of the cyclone reforming reactor; a third oxygen-enriched/water steam gas inlet is formed in the bottom of the material returning device. According to the device disclosed by the utility model, the problems of an existing biomass gasification process that the calorific value of the produced gas is low and the tar concentration of the produced gas is high can be effectively solved and various types of high-quality combustible gas capable of being directly applied to gas equipment can be prepared. The system can be operated in a self-heating manner, the gasification cost is low and the energy utilization rate is high.
Description
Technical field
The utility model relates to the device and method that low tar high heating value combustible gas is produced in a kind of biomass three-section type gasification, belongs to solid waste resource recovery and disposes field.
Background technology
Raising along with China's level of urbanization, the rural energy demand increases and changing appears in energy structure, household energy consumption structure in the countryside is changed to clean Sweet natural gas, LP gas fuel by traditional fuels such as stalk, fuel woods, and provincialism, seasonality and structural surplus appear in biomass resource.The upright burning disposal that connects of large number of biological, both wasted valuable resource, again severe contamination environment.Therefore, outlet is disposed in the processing that how to solve biomass, realizes the high efficiente callback utilization of biomass energy, has become significant problem urgently to be resolved hurrily in Chinese society doctrine new countryside construction.
Gasification is that solid fuel is converted into the process of combustible gas by the thermochemistry mode.Biomass gasification technology only needs a small amount of agriculture and forestry organic waste material just can produce inflammable gas, can specific aim solve the problems such as the rural area biomass processes is difficult, the universal difficulty of Sweet natural gas, energy scarcity problem for alleviating in the Rural Areas at Present process of economic development, alleviate environmental pollution and the wasting of resources and have important strategic importance.
Existing biomass gasification reaction device comprises the patterns such as fixed bed, fluidized-bed and air flow bed.Fixed-bed gasification furnace is simple in structure, less investment, easy to operate, but industrial scale is less and continuous operating performance is poor; Air flow bed is oxygen gasified to be generated the medium combustible gas of tar content and has higher efficiency of carbon conversion, and cost of investment is higher, is applicable to very large-scale gasification installation.Compare fixed bed or entrained flow gasification, fluidized-bed gasification has that heat and mass speed is high, suitability of fuel is wide, economy is high, easily amplify and the advantage such as mass-producing, receives increasing concern.
There is the problem that the aerogenesis tar-concentration is high, calorific value is low in existing fluidized bed gasification reactor, and the gasification aerogenesis need add expensive follow-up purification apparatus just can be used.Improve gasification temperature and can promote coke tar cracking, but increased simultaneously the risk of ash content slagging scorification and reduced gasification efficiency; By optimizing the vaporized chemical composition, can reduce tar-concentration, directly substitute but still can not meet combustible gas the requirement of using; Catalyzer affected by hydrokinetics and the catalyzer physical strength is low, poor heat stability, the easily restriction of poisoning and deactivation problem, applies more difficult; The sectional type gasification is mainly applied at present in the fixed bed gasification system, but the gasification of fluidized-bed sectional type more is conducive to improve gasification gas production rate and aerogenesis quality.
Summary of the invention
Technical problem:
For the problem that the aerogenesis calorific value is low, tar-concentration is high existed in current biomass gasification technology, the utility model proposes a kind of by the separated syllogic gasification installation of biomass pyrolytic, coke tar reforming and coke gasification, can produce low tar high heating value combustible gas, and gasification efficiency is high.
Technical scheme:
The device of low tar high heating value combustible gas is produced in biomass three-section type gasification of the present utility model, by fluidized bed gasification reactor, whirlwind reforming reactor, moving bed catalytic reactor and material returning device, formed, fluidized bed gasification reactor top and whirlwind reforming reactor top link, the fluidized bed gasification reactor bottom links by material returning device and moving bed catalytic reactor bottom, and whirlwind reforming reactor top and moving bed catalytic reactor top link; The fluidized bed gasification reactor bottom also is provided with biological particles charging opening and the first oxygen enrichment/water vapour inlet mouth, and the fluidized bed gasification reactor bottom is provided with slag-drip opening; Whirlwind reforming reactor top is the second oxygen enrichment/water vapour inlet mouth, and whirlwind reforming reactor bottom is the slag tap mouth; The moving bed catalytic reactor bottom is provided with coke import and combustible gas outlet, and the moving bed catalytic reactor bottom is provided with ash discharging hole; The material returning device bottom is three oxygen enrichment/water vapour inlet mouth.
The utility model is produced the method for low tar high heating value combustible gas, comprises the steps:
(1) to fluidized bed gasification reactor, send into biomass material, oxygen enrichment/water vapour, under 600 ~ 800 ℃ of conditions, generate thick matter combustible gas and pyrolysis coke, thick matter combustible gas is transported to the whirlwind reforming reactor by fluidized bed gasification reactor top, pyrolysis coke is transported to moving bed catalytic reactor by the fluidized bed gasification reactor bottom through material returning device, the material returning device bottom passes into the continuous conveying that oxygen enrichment/water vapour guarantees coke granule, and the end slag that gasification generates is discharged by the fluidized bed gasification reactor slag-drip opening;
(2) after thick matter combustible gas enters the whirlwind reforming reactor, simultaneously in the second oxygen enrichment/water vapour inlet mouth, pass into oxygen enrichment/water vapour, under the condition of 1200 ~ 1400 ℃, thick matter combustible gas removes tar and the high-temperature combustible gas that is purified of ash content wherein, by whirlwind reforming reactor top, be transported to moving bed catalytic reactor, the slag that reaction generates is discharged by the slag tap mouth of whirlwind reforming reactor;
(3) pyrolysis coke heap-shaped coke bed in moving bed catalytic reactor, after high-temperature combustible gas after reformation enters moving bed catalytic reactor, tar further cracking under the coke catalysis atmosphere of 700 ~ 900 ℃ removes, and pyrolysis coke is by the CO in high-temperature combustible gas
2And aqueous vapour reducing generation CO, the low tar high heating value combustible gas obtained after catalytic reduction is discharged by the outlet of moving bed catalytic reactor bottom combustible gas, and gasification produces ash content and is discharged by bottom ash discharging hole.
The temperature of reaction of described fluidized bed gasification reactor is 750 ℃, and whirlwind reforming reactor temperature of reaction is 1200 ℃, and the moving bed catalytic reactor temperature of reaction is 880 ℃.
Oxygen enrichment/the water vapour passed into is the mixed gas of oxygen rich gas and water vapour, and the ratio of mixed gas is 1:1 ~ 5:1, and oxygen rich gas concentration is 40%; 400 ~ 500 ℃ of steam temperatures.
The method of low tar high heating value combustible gas is produced in syllogic gasification of the present utility model, biological particles is added in fluidized-bed, biological particles and water vapour, oxygen rich gas acutely mix, strong heat and mass exchange occur, make the biological particles in bed rise to rapidly an interior temperature, in biomass, volatile matter and tar are separated out in the Mierocrystalline cellulose pyrolysis, and xylogen decomposes the generation coke granule.Carrying the thick matter combustible gas of a large amount of tar and ash content and delivering to the whirlwind reforming reactor by fluidized-bed top, coke is delivered to moving bed catalytic reactor as catalyzer by the fluidized-bed bottom through material returning device.The material returning device bottom passes into oxygen rich gas and water vapour is regulated operational throughput, guarantees the continuous transmission of coke granule and avoids the gas anti-channeling.In the whirlwind reforming reactor, the thick matter combustible gas of part and oxygen rich gas generation combustion reactions maintain the reformation high-temperature atmosphere, elementary tar is removed by thorough cracking through Pintsch process and steam reforming reaction, and the ash content high-temperature fusion is discharged by slag-drip opening after forming liquid lime-ash.Heavy metal in ash content can be stablized and admittedly is fused in slag, and slag is landfill or as building and roadbed material directly.Pyrolysis coke is sent in moving bed catalytic reactor and is piled up and become coke bed, and the high-temperature combustible gas after reformation is sent into and heat is passed in moving-bed by the moving-bed top.Tar fully contacts and the catalyzed micro-molecular gas that is cracked into coke, and coke is by the water vapour in combustible gas and CO simultaneously
2Reform and generate CO, aerogenesis cleanliness factor and calorific value all are improved.In contrive equipment, by the vaporized chemical component of each section that syllogic is gasified and the adjusting of operating parameter, the combustible gas that availability matter is different, meet the requirement of the various gas application such as engine, internal combustion turbine and chemical industry synthesize.Oxygen rich gas and combustible gas burning can be the system heat supply, realize the autothermal operation of system.
Beneficial effect:
The efficiency of carbon conversion of conventional fluidisation bed gasification technology is low and gas tar oil concentration is higher, the follow-up purifying treatment difficulty of gas.The utility model is in conjunction with the technical superiority of existing high-temperature gasification, oxygen enrichment/steam reforming, sectional type gasification and catalytic pyrolysis, propose a kind of novel three-stage gasifying biomass and produce the device and method of low tar high heating value combustible gas, biomass pyrolytic, coke tar reforming and coke gasification process are separated, can effectively be improved tar and coke transformation efficiency.The demonstration of syllogic gasification analog result, when fluidized-bed temperature is 750 ℃, whirlwind reforming reaction actuator temperature is 1200 ℃, and when the moving-bed temperature was 880 ℃, the syllogic gasification efficiency can reach 81%, and the coke transformation efficiency is 98%, and the coal-tar middle oil content of aerogenesis is low to moderate 10mg/Nm
3.Therefore, the utility model can reduce combustible gas secondary-cleaned cost, realizes the direct application of aerogenesis on gas-fired equipment.
1, fluidized-bed gasification is applicable to the fuel of multiple different qualities and easily amplifies, by middle low temperature pyrogenation gasification, can avoid the fluidized-bed fluctuation of service that in biomass, the ash content slagging scorification causes, adopt oxygen enrichment/steam gasification to generate and contain tar more thick matter combustible gas and pyrolysis coke.Oxygen-rich gasification can improve gasification reaction speed and gasification efficiency, and is the steam reforming reaction heat supply, reduces the use of external heat source, and steam reforming helps to reduce tar yield.The pyrolysis coke carbon content is high, can be used as good tar cracking catalyst.
2, the whirlwind reforming reactor is reformed to the tar in thick matter combustible gas under high temperature+steam atmosphere, and passing into of water vapour can prevent reforming reactor coking and tar generation after polymerization.The ash content high-temperature fusion is liquid lime-ash, and the pollutents such as effectively admittedly molten heavy metal, slag be landfill or reclaim as building and roadbed material directly.Reactor high temperature atmosphere maintains by the thick matter combustible gas burning of oxygen rich gas and part heat release, has reduced the use of fossil oil, has reduced running cost.
3, pyrolysis coke is directly used in performing catalytic pyrolysis on tar in moving-bed, can further reduce tar-concentration, save the catalyzer use cost, has also solved coal-tar middle oil, the problem that catalytic effect not good short with coke duration of contact of fluidized-bed gasification.Simultaneously, coke also can be by water vapour and CO
2Further gasification generates CO, and tar and coke transformation efficiency all are improved.
4, adopt material returning device to realize that pyrolysis coke, by the continuous transmission of fluidized bed gasification reactor to moving bed catalytic reactor, effectively avoids the gas anti-channeling.The material returning device bottom passes into oxygen rich gas and water vapour is regulated operational throughput, guarantees the continuous transmission of coke granule.The difference of based on fuel activity and ash content, material returning device can be used as microburner (logical oxygen rich gas) or reforming reactor (water flowing steam) is used, the requirement that the adaptive system operation condition changes.
5, the syllogic gasification system that adopts fluidized-bed, high temperature to reform and combine with moving-bed, flexible and convenient operation, the combustible gas that vaporized chemical component that can be by adjusting each section process and operational conditions are obtained number of different types, meet the requirement of the different combustion gas application such as prepared by internal combustion turbine, engine and chemical industry.Compare fixed bed segmented gasification throughput larger, be more suitable for medium-sized or large industrialized production, commercial applications has good prospects.
6, gasify and the oxygen concn of the oxygen rich gas used of reforming in 40% left and right, can obtain by oxygen enrichment membrane type oxygen generation method, the oxygen cost is lower.Passing into as fluidized-bed and reforming reactor provide institute's heat requirement of oxygen rich gas, after reforming, the heat of high-temperature combustible gas is passed to moving-bed to maintain catalysis temperature required, and whole gasification system can be realized the autothermal operation.
The accompanying drawing explanation
Fig. 1 is biomass three-section type gasifying process schematic flow sheet of the present utility model.
Fig. 2 is the temperature variant graphic representation of gasification property.
Fluidized bed gasification reactor 1 is wherein arranged, screw feeder 1-1, air compartment 1-2, air distribution plate 1-3, whirlwind reforming reactor 2, moving bed catalytic reactor 3, material returning device 4, the first oxygen enrichments/water vapour inlet mouth A, biological particles charging opening B, slag-drip opening C, the second oxygen enrichment/water vapour inlet mouth D, slag tap mouth E, coke import F, combustible gas outlet G, ash discharging hole H, three oxygen enrichment/water vapour inlet mouth I.
Embodiment
Low tar high heating value combustible gas device is produced in the biomass three-section type gasification that the utility model provides, and mainly fluidized bed gasification reactor 1, whirlwind reforming reactor 2, moving bed catalytic reactor 3 and material returning device 4, consists of.Fluidized bed gasification reactor 1 top and whirlwind reforming reactor 2 tops link, and bottom links by material returning device 4 and moving bed catalytic reactor 3 bottoms, and whirlwind reforming reactor 2 tops and moving bed catalytic reactor 3 tops link.The bottom of fluidized bed gasification reactor 1 also is provided with biological particles charging opening B and the first oxygen enrichment/water vapour inlet mouth A, and bottom is provided with slag-drip opening C; Whirlwind reforming reactor 2 tops are the second oxygen enrichment/water vapour inlet mouth D, and bottom is slag tap mouth E; Moving bed catalytic reactor 3 bottoms are provided with coke import F and combustible gas outlet G, and bottom is provided with ash discharging hole H; Material returning device 4 bottoms are three oxygen enrichment/water vapour inlet mouth I.
The detailed process of preparation method is: biological particles is added by biological particles charging opening B through screw feeder 1-1, oxygen enrichment/steam gasification agent is passed into by the first oxygen enrichment/water vapour inlet mouth A, and biological particles carries out pyrolytic gasification and reacts in fluidized bed gasification reactor 1 with oxygen enrichment/water vapour.In biomass, volatile matter and tar are separated out in the Mierocrystalline cellulose pyrolysis, and xylogen decomposes the generation coke granule, and lime-ash is discharged through slag-drip opening C.The thick matter combustible gas that gasification generates is carrying tar and ash content is left by fluidized bed gasification reactor 1 top, enters in whirlwind reforming reactor 2.The coke granule that gasification generates flows into material returning device 4, and under the effect from three oxygen enrichment/oxygen enrichment/water vapour that water vapour inlet mouth I passes into, coke granule is sent in moving bed catalytic reactor 3 and is used as catalyzer by coke import F.Oxygen enrichment/water vapour that the second oxygen enrichment/water vapour inlet mouth D passes into by whirlwind reforming reactor 2, with the abundant mixing reforming of thick matter combustible gas, at high temperature cracking of tar or further remove with water vapour generation reforming reaction, the liquid lime-ash that the flying dust high-temperature fusion in combustible gas generates is discharged through slag tap mouth E.From whirlwind reforming reactor 2 high-temperature combustible gas out, enter moving bed catalytic reactor 3, the bed of the coke build-up of flowing through is also further purified.Tar fully contacts and catalyzed cracking with coke, and coke is at water vapour and CO
2Effect under be reduced and generate CO, clean combustible gas is discharged by moving-bed bottom combustible gas outlet G, residual ash is discharged by bottom ash discharging hole H.
In whole biomass three-section type gasification, fluidized bed gasification reactor is in the middle temperature state of 600 ~ 800 ℃, the whirlwind reforming reactor is in 1200 ~ 1400 ℃ of conditions of high temperature, and moving bed catalytic reactor maintains temperature in 700 ~ 900 ℃ by the high-temperature combustible gas transferring heat.Pyrolysis gas is reformed and is removed tar through high-temperature vapor, and pyrolysis coke is delivered to moving bed catalytic reactor as catalyzer, by biomass pyrolytic, coke tar reforming and coke gasification process separately, is the system heat supply by oxygen-rich gasification, realizes the autothermal operation of system.
Figure 2 shows that gasification efficiency, coke transformation efficiency and the coal-tar middle oil content of aerogenesis of the analog calculation change curve with gasification temperature.Analog result shows, gasification efficiency, coke transformation efficiency raise and increase gradually with temperature, temperature more than 1000 ℃ gasification efficiency reach more than 80%, the coke transformation efficiency can reach more than 90%; Tar yield raises and significantly descends with temperature, is reduced to 10mg/Nm 1200 ℃ of left and right
3.Due to the restriction of fluidized-bed temperature easy coking and blocking when too high, in gasification in the past, the gasification temperature general control, below 820 ℃, causes gasification efficiency and coke low conversion rate, tar yield higher, has affected the direct use of gasification gas.By the syllogic gasification process, can when avoiding coking, the gasifying biomass temperature be increased to 1200 ~ 1400 ℃, gasification efficiency and coke transformation efficiency all can reach higher level, and tar yield also will decline to a great extent.
Claims (1)
1. the device of low tar high heating value combustible gas is produced in biomass three-section type gasification, by fluidized bed gasification reactor (1), whirlwind reforming reactor (2), moving bed catalytic reactor (3) and material returning device (4), formed, it is characterized in that: fluidized bed gasification reactor (1) top and whirlwind reforming reactor (2) top link, fluidized bed gasification reactor (1) bottom links by material returning device (4) and moving bed catalytic reactor (3) bottom, and whirlwind reforming reactor (2) top and moving bed catalytic reactor (3) top link; Fluidized bed gasification reactor (1) bottom also is provided with biological particles charging opening (B) and the first oxygen enrichment/water vapour inlet mouth (A), and fluidized bed gasification reactor (1) bottom is provided with slag-drip opening (C); Whirlwind reforming reactor (2) top is the second oxygen enrichment/water vapour inlet mouth (D), and whirlwind reforming reactor (2) bottom is slag tap mouth (E); Moving bed catalytic reactor (3) bottom is provided with coke import (F) and combustible gas outlet (G), and moving bed catalytic reactor (3) bottom is provided with ash discharging hole (H); Material returning device (4) bottom is three oxygen enrichment/water vapour inlet mouth (I).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305285A (en) * | 2013-06-17 | 2013-09-18 | 东南大学 | Device and method for preparing low-tar high-heat-value combustible gas by three-section-type gasification of biomass |
| CN104449845A (en) * | 2014-12-05 | 2015-03-25 | 盐城环波能源科技有限公司 | Biomass waste sealed quantitative feeding device and using method thereof |
| WO2019078787A1 (en) | 2017-10-19 | 2019-04-25 | Kosonsittiwit Phakorn | An apparatus for fuel gas production and combustion |
| WO2023161407A1 (en) * | 2022-02-25 | 2023-08-31 | Gidara Energy B.V. | Plant, device and process |
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2013
- 2013-06-17 CN CN2013203433392U patent/CN203307297U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305285A (en) * | 2013-06-17 | 2013-09-18 | 东南大学 | Device and method for preparing low-tar high-heat-value combustible gas by three-section-type gasification of biomass |
| CN103305285B (en) * | 2013-06-17 | 2014-10-15 | 东南大学 | Device and method for preparing low-tar high-heat-value combustible gas by three-section-type gasification of biomass |
| CN104449845A (en) * | 2014-12-05 | 2015-03-25 | 盐城环波能源科技有限公司 | Biomass waste sealed quantitative feeding device and using method thereof |
| CN104449845B (en) * | 2014-12-05 | 2016-09-14 | 盐城环波能源科技有限公司 | A kind of biomass garbage closed type metering device and using method |
| WO2019078787A1 (en) | 2017-10-19 | 2019-04-25 | Kosonsittiwit Phakorn | An apparatus for fuel gas production and combustion |
| EP3697748A4 (en) * | 2017-10-19 | 2021-07-28 | Kosonsittiwit, Phakorn | An apparatus for fuel gas production and combustion |
| WO2023161407A1 (en) * | 2022-02-25 | 2023-08-31 | Gidara Energy B.V. | Plant, device and process |
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