CN102154031A - Biomass gasification system - Google Patents
Biomass gasification system Download PDFInfo
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- CN102154031A CN102154031A CN2011100547664A CN201110054766A CN102154031A CN 102154031 A CN102154031 A CN 102154031A CN 2011100547664 A CN2011100547664 A CN 2011100547664A CN 201110054766 A CN201110054766 A CN 201110054766A CN 102154031 A CN102154031 A CN 102154031A
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Abstract
The invention belongs to energy equipment and particularly relates to a biomass gasification system. The system comprises an air supply system, a spiral feeder, a fluidized bed gasification furnace, a cyclone separator, a tar reformer, a purification system and a gas storage device. At least three sample inlets for introduction of gas or addition of solid catalystsare arranged in one side of the wall of the fluidized bed gasification furnace, and at least two sample inlets for addition of liquid catalysts are arranged in a blind plate. After biomass is gasified, unreacted biomass is separated out by the separation of cyclone separator so as to play a role in primarily purifying pyrolysis gas, the pyrolysis gas is processed by the tar reformer to convert most of tar into permanent gas, the permanent gas is processed by the purification system to further remove little unconverted macromolecular tar and other unconverted substances, and pure pyrolysis gas can be obtained and sent to the gas storage device or supplied to gas users directly. The gasification system has the advantages of simple structure, safety, reliability and strong controllability, can be used for gasifying various biomass fuels and is suitable for areas rich in biomass resources.
Description
Technical field
The invention belongs to energy device, relate in particular to a kind of biomass gasification system.
Background technology
Characteristics such as widely distributed, renewable and environmental friendliness that biomass energy has, the development and use renewable resources is the main direction that China realizes Sustainable development.Current, the biomass energy transformation technology mainly is divided into gasifying biomass, liquefaction, curing and direct combustion technology.The biomass energy gasification technology is one of important method wherein.Realize the profound level utilization of low-grade biomass energy with gasification mode, reduce the supply of mineral fuel and directly use the severe contamination that mineral fuel bring to environment, to raising life in the countryside level, improve the ecological environment, ensure that national energy security etc. is significant
Biomass make it become the desirable feedstock of gasification owing to have characteristics such as the content of volatilization component content height, carbon activity height, sulphur, nitrogen and ash is low.With Wood Adhesives from Biomass is that inflammable gas is the fine approach of biomass utilization.The type of furnace that present domestic gasifying biomass adopted generally comprises fixed-bed gasification furnace and fluidized-bed gasification furnace.But fixed-bed gasification furnace is because throughput is little, tar output is big, gasification efficiency is low and can not carry out shortcoming such as large-scale industrial production and do not used on a large scale.And fluidized-bed gasification furnace since gasification efficiency height, raw material wide accommodation, synthetic gas tar content are low and can the heavy industrialization application etc. advantage become the preferred manner of gasification.
At present, there is complex structure in a lot of biomass gasification devices that put into operation, running cost height, biomass kind bad adaptability, problem such as gasification efficiency is low, and tar output is big.
Summary of the invention
The objective of the invention is in order to overcome the various defectives of existing gasification technology, provide a kind of simple in structure, running cost is low, gasification efficiency is high, the biomass gasification system of good purification.
The present invention is achieved through the following technical solutions:
This gasification system is made of supply air system, screw feeder, fluidized-bed reactor, cyclonic separator, coke tar reforming device, purification system and accumulator unit.Described supply air system comprises fan, air supply duct and the air compartment that connects successively, and the air distribution plate that is arranged on the air compartment top; Be provided with cinder notch around the air distribution plate, lime-ash is discharged by the grey slag bucket of the cinder notch below that falls; The top of described air distribution plate is a fluidized-bed reactor; The outlet of described screw feeder is connected with the inlet of fluidized-bed reactor; The outlet of described fluidized-bed reactor links to each other with cyclonic separator; Cyclonic separator is by coke tar reforming device and purification system UNICOM; Wherein, purification system is made of the cyclic water tank of spray column, spray column below, the water circulating pump of cyclic water tank bottom and the pipeline that water circulating pump is connected with spray column; The purification system pneumatic outlet be connected with accumulator unit with the gas user respectively.
The described cinder notch that falls is a ring structure.
Described grey slag bucket, air compartment are integrated, and air compartment is positioned at grey slag bucket inside.
The sidewall of described fluidized-bed reactor is provided with 3 solids or gas sampling mouth at least.
Described fluidized-bed reactor sidewall leaves 5 solids or gas sampling mouth.
The top of described fluidized-bed reactor is provided with blind plate, and is left to rare two liquid injection ports on blind plate.
Leave two liquid injection ports on the described blind plate.
Described spray column adopts the high atomization shower nozzle.
Described cyclic water tank inside is divided into two, about two districts bottoms UNICOM become U type structure.
Described cyclic water tank is semi-enclosed water tank, and water tank one side is the tar collecting region, and an other side is pure recirculated water source region.
Temperature is 600～900 ℃ in the fluidized-bed reactor stove; The biomass raw material particle particle diameter is 2mm～20mm; The gasification efficiency of fluidized-bed reactor is 70%～85%.
The present invention has the following advantages:
1. the present invention adopts is the annular slag mode that falls, and lime-ash and unreacted particle are discharged by grey slag bucket by the cinder notch that falls of the annular around the air distribution plate, have avoided ash deposition around air distribution plate, influence the works better of air distribution plate.
2. air compartment of the present invention is positioned at grey slag bucket inside, and cold wind is heated in grey slag bucket inside, can recycle cindery waste heat, has increased wind pushing temperature again, helps improving the whole efficiency of system.
3. fluidized-bed reactor one side of the present invention leaves and leaves 2 injection ports on 5 injection ports, the blind plate, can select to add different gasifying medium or catalyzer according to different biomass materials.
4. cyclic water tank of the present invention adopts the U type structure of bottom UNICOM, utilizes the density difference of tar and water and uncompatibility to separate tar from water.
5. the present invention adopts fluidized-bed reactor, coke tar reforming and purification way of combining, and the pyrolysis gas tar content of generation is very low, is convenient to pyrolysis gas is fully utilized.
6. the present invention adopts the mode of gas user and accumulator unit and usefulness, is convenient to operation, and safe and reliable, controllability is strong.
Description of drawings
Fig. 1 is the structural representation of fluidized-bed gasification furnace of the present invention;
Fig. 2 is a structural representation of the present invention.
Number in the figure:
The I-supply air system; The II-screw feeder; The III-fluidized-bed gasifier; The IV-cyclonic separator; V-coke tar reforming device; The VI-purification system; The VII-accumulator unit; The 1-fan; The 2-air supply duct; The 3-air compartment; The 4-air distribution plate; 5-gas user; The 6-spray column; The 7-cyclic water tank; The 8-water circulating pump; 9-ash slag bucket; The 10-cinder notch that falls; 11-solid or gas sampling mouth; The 12-blind plate; 13-liquid injection port.
Embodiment
The invention provides a kind of biomass gasification system, the present invention will be further described below by the drawings and specific embodiments.
As depicted in figs. 1 and 2, this gasification system is made of supply air system I, screw feeder II, fluidized-bed reactor III, cyclonic separator IV, coke tar reforming device V, purification system VI and accumulator unit VII.Wherein, supply air system I comprises fan 1, air supply duct 2 and the air compartment 3 that connects successively, and the air distribution plate 4 that is arranged on air compartment 3 tops; Be provided with cinder notch 10 around the air distribution plate 4, lime-ash is discharged by the grey slag bucket 9 of cinder notch 10 belows that fall; The top of described air distribution plate 4 is fluidized-bed reactor III; The outlet of described screw feeder II is connected with the inlet of fluidized-bed reactor III; The outlet of described fluidized-bed reactor III links to each other with cyclonic separator IV; Cyclonic separator IV is by coke tar reforming device V and purification system VI UNICOM; Wherein, purification system VI constitutes with the pipeline that spray column 6 is connected by the water circulating pump 8 of the cyclic water tank 7 of spray column 6, spray column 6 belows, cyclic water tank 7 bottoms and with water circulating pump 8; Purification system VI pneumatic outlet be connected with accumulator unit VII with gas user 5 respectively.
The cinder notch 10 that falls is ring structure, and grey slag bucket 9, air compartment 3 are integrated, and air compartment 3 is positioned at grey slag bucket 9 inside.The sidewall of fluidized-bed reactor III is provided with 3 solids or gas sampling mouth 11 at least.The top of fluidized-bed reactor III is provided with blind plate 12, and is left to rare two liquid injection ports 13 on blind plate 12.Adopt the high atomization shower nozzle in the spray column 6.Cyclic water tank 7 is semi-enclosed water tank, and inside is divided into two, and a side is the tar collecting region, and an other side is pure recirculated water source region, about two districts bottoms UNICOM become U type structure
Temperature is 600～900 ℃ in the fluidized-bed reactor stove; The biomass raw material particle particle diameter is 2mm～20mm; The gasification efficiency of fluidized-bed reactor is 70%～85%.
Embodiment 1
Is example with 600 ℃ of furnace temperature, air equivalent than 0.15.
The biomass material of different-grain diameter enters fluidized-bed reactor III by screw feeder II, biomass material advanced screw feeder II and was compressed the tap density increase, effectively prevent collaborate (201010259031.0) between screw feeder II and the fluidized-bed reactor III, air is sent into fluidized-bed reactor III by air compartment by air distribution plate 4 by fan 1, is 0.15 by the big or small control air equivalence ratio of regulating glass patent under meter.Raw material is being in fluidized state and generating gasification reaction generation CO, H under 600 ℃ of temperature under the fluidisation wind action
2, CH
4, CO
2And N
2Deng gas.Solid waste falls into grey slag bucket 9 by the annular cinder notch 10 that falls, and discharges by scum pipe.The pyrolysis gas that generates at first carries out rough purification by cyclonic separator IV, and the solid particulate of separating is discharged by slag dropping tube.By coke tar reforming device V, the tar in the pyrolysis gas is catalytically conveted to permanent gases then, does further purifying treatment through purification system VI again afterwards, and the clean pyrolysis gas in process a series of purifications back is delivered to gas user 5 or sends among the accumulator unit VII.The content of CO is 25% in the pyrolysis gas that generates, H
2Content be 8%, CH
4Content be 9%, CO
2Content be 15%, N
2Content be 41%, gasification efficiency is 70%.Transformation efficiency reaches 95% behind the tar process coke tar reforming device.
Embodiment 2
Is example with 700 ℃ of furnace temperature, air equivalent than 0.22.
According to embodiment 1 described flow process, biomass generating gasification reaction under 700 ℃ of temperature generates CO, H when the air equivalent ratio is 0.22
2, CH
4, CO
2And N
2Deng gas.The content of CO is 21% in the synthetic gas that generates, H
2Content be 6%, CH
4Content be 6%, CO
2Content be 15.3%, N
2Content be 49%, gasification efficiency is 74%.Transformation efficiency reaches 96% behind the tar process coke tar reforming device.
Embodiment 3
Is example with 800 ℃ of furnace temperature, air equivalent than 0.29.
According to embodiment 1 described flow process, biomass generating gasification reaction under 800 ℃ of temperature generates CO, H when the air equivalent ratio is 0.29
2, CH
4, CO
2And N
2Deng gas.The content of CO is 18% in the synthetic gas that generates, H
2Content be 5%, CH
4Content be 5.6%, CO
2Content be 16%, N
2Content be 58%, gasification efficiency is 78%.Transformation efficiency reaches 99% behind the tar process coke tar reforming device.
Embodiment 4
Is example with 600 ℃ of furnace temperature, fluidized-bed gasification furnace III wall one side solid or gas sampling mouth bottom as the water vapour injection port.
The biomass material of different-grain diameter enters fluidized-bed reactor III by screw feeder II, biomass material advanced screw feeder II and was compressed the tap density increase, effectively prevent collaborating between screw feeder II and the fluidized-bed reactor III, air is sent into fluidized-bed reactor III by air compartment by air distribution plate 4 by fan 1, water vapour by fluidized-bed gasification furnace III wall one side bottom injection port feed in the stove.Raw material generating gasification reaction under 600 ℃ of temperature generates CO, H
2, CH
4, CO
2And C
2H
4Deng gas.Solid waste falls into grey slag bucket 9 by the annular cinder notch 10 that falls, and discharges by scum pipe.The pyrolysis gas that generates at first carries out rough purification by cyclonic separator IV, and the solid particulate of separating is discharged by slag dropping tube.By coke tar reforming device V, the tar in the pyrolysis gas is catalytically conveted to permanent gases then, does further purifying treatment through purification system VI again afterwards, and the clean pyrolysis gas in process a series of purifications back is delivered to gas user 5 or sends among the accumulator unit VII.The content of CO is 43% in the pyrolysis gas that generates, H
2Content be 21%, CH
4Content be 10%, CO
2Content be 20%, C
2H
4Content be 5%, gasification efficiency is 78%.Transformation efficiency reaches 96% behind the tar process coke tar reforming device.
Embodiment 5
Is example with 700 ℃ of furnace temperature, fluidized-bed gasification furnace III wall one side intermediary solid or gas sampling mouth as the water vapour injection port.
According to embodiment 4 described flow processs, when water vapour injection port in the middle of fluidized-bed gasification furnace III wall one side entered fluidized-bed gasification furnace III, biomass generating gasification reaction under 700 ℃ of temperature generated CO, H
2, CH
4, CO
2And C
2H
4Deng gas.The content of CO is 40% in the synthetic gas that generates, H
2Content be 27%, CH
4Content be 9%, CO
2Content be 19%, C
2H
4Content be 4%, gasification efficiency is 80%.Transformation efficiency reaches 97% behind the tar process coke tar reforming device.
Embodiment 6
Is example with 800 ℃ of furnace temperature, fluidized-bed gasification furnace III wall one side solid or gas sampling mouth topmost as the water vapour injection port.
According to embodiment 4 described flow processs, when water vapour when topmost injection port enters fluidized-bed gasification furnace III from fluidized-bed gasification furnace III wall one side, biomass generating gasification reaction under 800 ℃ of temperature generates CO, H
2, CH
4, CO
2And C
2H
4Deng gas.The content of CO is 38% in the synthetic gas that generates, H
2Content be 32%, CH
4Content be 8%, CO
2Content be 17%, C
2H
4Content be 3.5%, gasification efficiency is 85%.Transformation efficiency reaches 99% behind the tar process coke tar reforming device.
Claims (10)
1. biomass gasification system, constitute by supply air system (I), screw feeder (II), fluidized-bed reactor (III), cyclonic separator (IV), coke tar reforming device (V), purification system (VI) and accumulator unit (VII), it is characterized in that: described supply air system (I) comprises fan (1), air supply duct (2) and the air compartment (3) that connects successively, and the air distribution plate (4) that is arranged on air compartment (3) top; Be provided with cinder notch (10) around the air distribution plate (4), lime-ash is discharged by the grey slag bucket (9) of the cinder notch that falls (10) below; The top of described air distribution plate (4) is fluidized-bed reactor (III); The outlet of described screw feeder (II) is connected with the inlet of fluidized-bed reactor (III); The outlet of described fluidized-bed reactor (III) links to each other with cyclonic separator (IV); Cyclonic separator (IV) is by coke tar reforming device (V) and purification system (VI) UNICOM; Wherein, purification system (VI) is by the cyclic water tank (7) of spray column (6), spray column (6) below, the water circulating pump (8) of cyclic water tank (7) bottom and the pipeline formation that water circulating pump (8) is connected with spray column (6); Purification system (VI) pneumatic outlet be connected with accumulator unit (VII) with gas user (5) respectively.
2. biomass gasification system according to claim 1 is characterized in that: the described cinder notch (10) that falls is a ring structure.
3. biomass gasification system according to claim 1 is characterized in that: described grey slag bucket (9), air compartment (3) are integrated, and air compartment is positioned at grey slag bucket inside.
4. biomass gasification system according to claim 1 is characterized in that: the sidewall of described fluidized-bed reactor (III) is provided with 3 solids or gas sampling mouth (11) at least.
5. biomass gasification system according to claim 4 is characterized in that: described fluidized-bed reactor (III) sidewall leaves 5 solids or gas sampling mouth (11).
6. biomass gasification system according to claim 1 is characterized in that: the top of described fluidized-bed reactor (III) is provided with blind plate (12), and is left to rare two liquid injection ports (13) on blind plate (12).
7. want 6 described biomass gasification systems according to right, it is characterized in that: leave two liquid injection ports (13) on the described blind plate (12).
8. biomass gasification system according to claim 1 is characterized in that: described spray column (6) adopts the high atomization shower nozzle.
9. biomass gasification system according to claim 1 is characterized in that: described cyclic water tank (7) inside is divided into two, about two districts bottoms UNICOM become U type structure.
10. biomass gasification system according to claim 9 is characterized in that: described cyclic water tank (7) is semi-enclosed water tank, and water tank one side is the tar collecting region, and an other side is pure recirculated water source region.
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| CN2011100547664A CN102154031A (en) | 2011-03-08 | 2011-03-08 | Biomass gasification system |
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|---|---|---|---|
| CN2011100547664A CN102154031A (en) | 2011-03-08 | 2011-03-08 | Biomass gasification system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311747A (en) * | 2011-08-30 | 2012-01-11 | 河南宝舜化工科技有限公司 | Furnace-kettle type modified pitch production system and production process |
| CN102634355A (en) * | 2011-12-20 | 2012-08-15 | 华北电力大学 | Method for cracking biomass pyrolytic tar catalytically using nickel-carrying carbon nano tube |
| CN103146432A (en) * | 2013-03-18 | 2013-06-12 | 华北电力大学 | Biomass pyrolysis gasification and tar catalytic cracking device and method |
| CN104371763A (en) * | 2014-10-17 | 2015-02-25 | 湖南谷力新能源科技股份有限公司 | Rice hull tristate decomposition system |
| CN105441137A (en) * | 2015-12-28 | 2016-03-30 | 北京神雾环境能源科技集团股份有限公司 | Gasification reactor |
| CN109294626A (en) * | 2018-12-07 | 2019-02-01 | 浙江工业大学 | A kind of production process and device of gasification of biomass preparing synthetic gas |
| CN113372956A (en) * | 2021-06-09 | 2021-09-10 | 东南大学 | Utilize integrative accuse dirty system of domestic waste gasification of U type reactor |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311747A (en) * | 2011-08-30 | 2012-01-11 | 河南宝舜化工科技有限公司 | Furnace-kettle type modified pitch production system and production process |
| CN102634355A (en) * | 2011-12-20 | 2012-08-15 | 华北电力大学 | Method for cracking biomass pyrolytic tar catalytically using nickel-carrying carbon nano tube |
| CN102634355B (en) * | 2011-12-20 | 2014-04-23 | 华北电力大学 | Method for cracking biomass pyrolytic tar catalytically using nickel-carrying carbon nano tube |
| CN103146432A (en) * | 2013-03-18 | 2013-06-12 | 华北电力大学 | Biomass pyrolysis gasification and tar catalytic cracking device and method |
| CN104371763A (en) * | 2014-10-17 | 2015-02-25 | 湖南谷力新能源科技股份有限公司 | Rice hull tristate decomposition system |
| CN105441137A (en) * | 2015-12-28 | 2016-03-30 | 北京神雾环境能源科技集团股份有限公司 | Gasification reactor |
| CN105441137B (en) * | 2015-12-28 | 2017-12-08 | 神雾科技集团股份有限公司 | Gasification reactor |
| CN109294626A (en) * | 2018-12-07 | 2019-02-01 | 浙江工业大学 | A kind of production process and device of gasification of biomass preparing synthetic gas |
| CN109294626B (en) * | 2018-12-07 | 2024-06-25 | 浙江工业大学 | Production process and device for preparing synthesis gas by biomass gasification |
| CN113372956A (en) * | 2021-06-09 | 2021-09-10 | 东南大学 | Utilize integrative accuse dirty system of domestic waste gasification of U type reactor |
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