CN203128183U - System for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis - Google Patents
System for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis Download PDFInfo
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- CN203128183U CN203128183U CN2012207021293U CN201220702129U CN203128183U CN 203128183 U CN203128183 U CN 203128183U CN 2012207021293 U CN2012207021293 U CN 2012207021293U CN 201220702129 U CN201220702129 U CN 201220702129U CN 203128183 U CN203128183 U CN 203128183U
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Abstract
The utility model provides a system for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis. The system comprises a biomass pretreatment drying unit (1), a steam low-temperature pyrolysis unit (2), a high-temperature cyclone separation unit (3), a steam catalytic reforming unit (4) and a hydrogen cooling, purifying and separation unit (5), wherein the biomass pretreatment drying unit (1) is sequentially connected with the steam low-temperature pyrolysis unit (2), the high-temperature cyclone separation unit (3), the steam catalytic reforming unit (4) and the hydrogen cooling, purifying and separation unit (5); and a gas outlet of the biomass pretreatment drying unit (1) is connected with the high-temperature cyclone separation unit (3). The system provided by the utility model improves the heat utilization rate in the pyrolysis process, reduces the content of dust and tar in the pyrolysis air in follow-up working sections, simplifies the production technology of active carbon and hydrogen, saves investment and realizes low energy consumption.
Description
Technical field
The utility model relates to technical field of chemistry and chemical engineering, is specifically related to the system that a kind of biomass steam low temperature pyrogenation is produced gac and hydrogen.
Background technology
The biomass low temperature pyrogenation refers in pyrolysis temperature more than 400 ℃, biomass macromole (xylogen, Mierocrystalline cellulose and hemicellulose etc.) is resolved into the thermochemistry transformation technology of small molecules fuel material (coke, inflammable gas and biomass coke tar) by thermal chemical reaction.Pyrolysis is biomass combustion and requisite starting stage of gasification.Its type can be divided into 400～650 ℃ low temperature pyrogenation by pyrolysis temperature, three kinds of the high temperature pyrolysis of warm solution and 850～1100 ℃ in 650～850 ℃.In pyrolytic process, because heat is earlier to be delivered to the material surface by thermal source, be delivered to material inside by the material surface again, thereby the pyrolytic process of biomass is successively to carry out from outside to inside, finally obtain biomass coke tar, inflammable gas and coke.The fuel energy transformation efficiency of biomass pyrolytic can be converted into energy product with biomass energy to greatest extent generally more than 90%.
At present, the biomass pyrogenation gasification technology that China uses mainly comprises fixed bed, fluidized-bed and direct three kinds of process forms of destructive distillation.Fixed bed gasification generally adopts air to make vaporized chemical, and device structure is simple, easy handling, less investment; But N in the biological fuel gas that obtains as vaporized chemical with air
2, O
2The content height, low (the about 5000kJ/Nm of calorific value
3), and the coal-tar middle oil content height of inflammable gas, easily blocking pipeline.Fluidized bed pyrolysis then most solid thermal carriers (heating sand) or gaseous heat-carriers of adopting provides heat for pyrolytic process; The drag force that main dependence gas motion produces between biological particles and thermal barrier is collided and is mixed, to realize momentum exchange and thermal exchange.Its advantage is not contain moving parts in the fluidized-bed, and simple in structure, operation life is long, and treatment capacity is big; But the introducing of fluidized gas has also improved the operation energy consumption cost of system, has increased the dust content in the gaseous product.And in the direct destructive distillation of ordinary student material, also exist the material heating rate slow, shortcoming such as it is inhomogeneous to be heated, and thermo-efficiency is low.On the one hand, because biomass coke tar is the hydrocarbon polymer of rich oxygen content, long time stored meeting be separated, precipitate, and has severe corrosive, thereby all have labile factor on physics, chemical property.On the other hand, volatile matter height, the fixed carbon content of biomass material are low, and unit weight is little, are unfavorable for gasification.Owing to be rich in hydrogen in the biomass, can produce H by process for making hydrogen such as cracking, self-heating recapitalization, steam reformations
2, but at biomass water vapour catalytic pyrolysis gasification H processed
2In the technology, exist heat and mass speed low again, granules of catalyst surface carbon deposit is serious, and inactivation is fast, a large amount of CO
2Generation has suppressed H processed
2React, reduced the H processed of biomass
2Efficient.
As seen seek new biomass energy efficient technique of rainwater utilization, with the effective constituent in the abundant extraction biomass material, improve the hot fields that existing Wood Adhesives from Biomass efficient is present biomass utilization research, produce gac and hydrogen is one of effective way of biomass energy comprehensive utilization with lignocellulose biomass.
The utility model content
The purpose of this utility model is to solve the subproblem that exists in the existing biomass pyrogenation gasification technology, and the exploitation biomass are the renewable lignocellulose biomass energy particularly, provides a kind of biomass water vapour low temperature pyrogenation to produce the system of gac and hydrogen.
The purpose of this utility model is achieved through the following technical solutions:
A kind of biomass steam low temperature pyrogenation is produced the system of gac and hydrogen, comprises biomass pre-treatment drying unit 1, water vapour low temperature pyrogenation unit 2, high temperature cyclonic separation unit 3, steam catalytic reforming unit 4, hydrogen cooling and purifying separating unit 5; Wherein, described biomass pre-treatment drying unit 1 connects water vapour low temperature pyrogenation unit 2 successively, high temperature cyclonic separation unit 3, steam catalytic reforming unit 4, hydrogen cooling and purifying separating unit 5, the pneumatic outlet of described biomass pre-treatment drying unit 1 is connected with high temperature cyclonic separation unit 3.
Described biomass pre-treatment drying unit 1 is provided with the porous kicker baffle that multilayer tilts.
Described kicker baffle percentage of open area is 20-30%, and the aperture is 1.5-3.0mm.
The angle of described kicker baffle and biomass material pre-treatment drying unit 1 perpendicular is 20 °-40 °, and the direction of adjacent inclined kicker baffle is opposite.
Described water vapour low temperature pyrogenation unit 2 is provided with the porous gas grid distributor, and the percentage of open area of gas distribution grid is 5-15%, and the aperture is 0.5-1.5mm.
Described steam catalytic reforming unit 4 comprises tubular oven device and high-temperature air burning device, and being burnt outside boiler tube by the high-temperature air burning device provides the heat of catalytic reforming reaction.
The specific embodiment that this system produces gac and hydrogen is as follows:
(1) biomass material is crushed to certain particle size (particle size range: after 5.0～20mm), send into pre-treatment in the biomass pre-treatment drying unit; Biomass material by porous kicker baffle and the flow through pyrolysis gas of kicker baffle and water vapour mixed gas counter current contact, heat exchange and be dried.
(2) dried material enters water vapour low temperature pyrogenation unit, and is evenly distributed on the porous gas grid distributor, and water vapour heats through the even gas distribution of porous plate and with the biological particles fluidisation.Because the thermal capacitance of water vapour is big, is dispersed in the hole between biological particles, make the temperature rise rate of biological particles accelerate pyrolysis rapidly.Micro-pressure operation is kept in water vapour low temperature pyrogenation unit, and the steam temperature that enters in the water vapour low temperature pyrogenation unit is 550～650 ℃, and material can guarantee that at the indoor stop 30～90min of water vapour low temperature pyrogenation water vapour fully activates coke.The fluidizing velocity of biological particles is critical fluidization velocity U
Mf1～3 times.Also may there be following reaction in the low temperature pyrogenation of biomass except the pyrolytic reaction of biomass self under steam atmosphere:
The gasification reaction that biomass and water vapour take place:
C+H
2O→CO+H
2
When water vapour is excessive, take place
CO+H
2O→CO
2+H
2
Two water reactions take place in biomass and water vapour under cold condition,
C+2H
2O→CO
2+2H
2
(3) high temperature pyrolysis gas (containing water vapor) is by behind the biomass pre-treatment drying unit, and part dust and tar in the pyrolysis gas are deposited in the biomass material surface, after the dedusting of high temperature cyclonic separation unit, enters steam catalytic reforming unit.
(4) pyrolysis gas steam catalytic reforming unit adopts the tubular oven device.Nickel-base catalyst is positioned in the tubular oven boiler tube, provides heat with the heat accumulating type high-temperature air burning device for the pyrolysis gas steam reformation.At the indoor generation catalytic reforming reaction of steam reformation, small molecules hydro carbons and oxygen-bearing organic matter continue to be cracked into CH to pyrolysis gas (containing water vapor) under the nickel-base catalyst effect
4, H
2, CO
2With micro-molecular gas such as CO, the hydrogen productive rate height of steam reformation process, greenhouse gas emissions are few.Under 500～850 ℃ of reforming temperatures, following reforming reaction can take place with water vapour in small molecules hydro carbons and oxygen-bearing organic matter,
2C
nH
m+2nH
2O→nCO
2+（n+m/2）CH
4
CH
4+2H
2O→CO
2+4H
2
(5) hydrogen-rich gas is delivered to follow-up workshop section separating hydrogen gas after the condensation of hydrogen cooling and purifying separating unit.
The beneficial effects of the utility model: the system that the biomass steam low temperature pyrogenation is produced gac and hydrogen combines biomass material drying, water vapour low temperature pyrogenation, coke steam activation and pyrolysis gas and water vapour catforming, not only improved the heat utilization efficiency in the pyrolytic process, the airborne dust of follow-up workshop section pyrolysis and tar content have been reduced, and simplified the production technique of gac and hydrogen, reduced investment, energy consumption is low.
Description of drawings
Fig. 1 is the process flow sheet that the utility model biomass steam low temperature pyrogenation is produced gac and hydrogen gas system
Embodiment
The utility model, the technical scheme among the embodiment is clearly and completely described below in conjunction with the accompanying drawing among the embodiment for better illustrating.
With reference to Fig. 1, present embodiment is that the biomass water at low temperature steam pyrolysis of raw material prepares gac and hydrogen is example with bark, stem shape farm crop and sawmilling etc., and the treatment capacity of raw material is 0.5t/h, and particle diameter is 5.0～10.0mm, and the as received basis moisture content is 15.0%.Embodiment comprises the processing step of following order:
(1) be that the biomass material of 5.0～10.0mm is sent into biomass pre-treatment drying unit 1 with particle diameter; Material moves down along the guiding porous barrier of biomass pre-treatment kiln, with pyrolysis gas and mixture of steam counter current contact, heat exchange and the drying by kicker baffle.The kicker baffle percentage of open area is 20.0%, and the aperture is 1.5mm;
(2) dried material enters water vapour low temperature pyrogenation unit 2, and is evenly distributed on the porous gas grid distributor of water vapour low temperature pyrogenation chamber 2, and the porous plate percentage of open area is 5.0%, and the aperture is 0.5mm.Temperature is that 550 ℃ water vapour thermal barrier passes through porous plate, with biological particles fluidisation and heating.The fluidizing velocity of particle is 2 times of its critical fluidization velocity; Because the thermal capacitance of water vapour is big, when it is dispersed in the particle hole, the particle temperature rise rate is increased, pyrolysis rapidly.The residence time of biomass in pyrolysis unit is 60min.
(3) high temperature pyrolysis gas (containing water vapor) is by behind the biomass material pre-treatment drying unit 1, part dust in the pyrolysis gas and tar deposition are on the biomass surface, pyrolysis gas after 3 dedustings of high temperature cyclonic separation unit, enters steam catalytic reforming unit 4 again.
(4) nickel-base catalyst is placed in the boiler tube of steam catalytic reforming unit 4, be under 750 ℃ the water vapour existence condition in temperature, small molecules hydro carbons in the pyrolysis gas and oxygen-bearing organic matter are cracked into CH in that catalytic reforming reaction takes place under the nickel-base catalyst effect in steam catalytic reforming unit 4
4, H
2, CO
2With micro-molecular gas such as CO.
(5) hydrogen-rich gaseous mixtures is delivered to the subsequent handling separating hydrogen gas after the 5 condensation dedustings of hydrogen cooling and purifying separating unit.
The utility model compared with prior art has the following advantages and progress:
(1) catalytic reforming reaction of the drying of biomass, water vapour low temperature pyrogenation, coke steam activation being produced gac and pyrolysis gas and water vapour combines, utilize the mixed gas of pyrolysis gas and water vapour that biomass material is carried out dry pre-treatment, can improve the heat utilization efficiency of pyrolytic process; In addition, pyrolysis gas can deposit part tar, impurity and ash content in the process of kiln of flowing through, and can reduce dust and tar content in the follow-up workshop section pyrolysis gas;
(2) use tubular oven, pyrolysis gas can obtain the hydrogen-rich gas of high heating value, strong reducing property after catalytic reforming;
(3) with the activator of water vapour as thermal barrier and Preparation of Activated Carbon, but single stage method is produced the gac of high-specific surface area, has saved the CO in traditional process for preparing active carbon
2Activation step has been simplified the production technique of gac;
(4) compare with traditional hydrogen technology, this method is produced the reduced investment of hydrogen, and energy consumption is low.
The above; it only is the preferable embodiment of the utility model; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; the variation that can expect easily or replacement all should be encompassed within the protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion with the protection domain of claims.
Claims (6)
1. a biomass steam low temperature pyrogenation is produced the system of gac and hydrogen, it is characterized in that, comprise biomass pre-treatment drying unit (1), water vapour low temperature pyrogenation unit (2), high temperature cyclonic separation unit (3), steam catalytic reforming unit (4), hydrogen cooling and purifying separating unit (5); Wherein, described biomass pre-treatment drying unit (1) connects water vapour low temperature pyrogenation unit (2) successively, high temperature cyclonic separation unit (3), steam catalytic reforming unit (4), hydrogen cooling and purifying separating unit (5), the pneumatic outlet of described biomass pre-treatment drying unit (1) is connected with high temperature cyclonic separation unit (3).
2. biomass steam low temperature pyrogenation according to claim 1 is produced the system of gac and hydrogen, it is characterized in that, described biomass pre-treatment drying unit (1) is provided with the porous kicker baffle that multilayer tilts.
3. the system that wants 2 described biomass steam low temperature pyrogenations to produce gac and hydrogen according to right is characterized in that described kicker baffle percentage of open area is 20-30%, and the aperture is 1.5-3.0mm.
4. want the system of 2 described biomass steam low temperature pyrogenations production gacs and hydrogen according to right, it is characterized in that, the angle of described kicker baffle and biomass material pre-treatment drying unit (1) perpendicular is 20 °-40 °, and the direction of adjacent inclined kicker baffle is opposite.
5. biomass steam low temperature pyrogenation according to claim 1 is produced the system of gac and hydrogen, it is characterized in that, described water vapour low temperature pyrogenation unit (2) is provided with the porous gas grid distributor, and the percentage of open area of gas distribution grid is 5-15%, and the aperture is 0.5-1.5mm.
6. biomass steam low temperature pyrogenation according to claim 1 is produced the system of gac and hydrogen, it is characterized in that, described steam catalytic reforming unit (4) comprises tubular oven device and high-temperature air burning device, and being burnt outside boiler tube by the high-temperature air burning device provides the heat of catalytic reforming reaction.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012207021293U CN203128183U (en) | 2012-12-18 | 2012-12-18 | System for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis |
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|---|---|---|---|
| CN2012207021293U CN203128183U (en) | 2012-12-18 | 2012-12-18 | System for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103011157A (en) * | 2012-12-18 | 2013-04-03 | 北京神雾环境能源科技集团股份有限公司 | System and method for producing activated carbon and hydrogen through low-temperature pyrolysis of biomass steam |
| CN106629710A (en) * | 2016-12-05 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | System and method for preparing activated carbon |
| CN106629715A (en) * | 2016-12-08 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | System and method for preparing active carbon by biomass |
| CN107416767A (en) * | 2017-08-16 | 2017-12-01 | 华中科技大学 | A kind of method that hydrogen and carbon electrode material are prepared using biomass |
| CN109852421A (en) * | 2019-02-25 | 2019-06-07 | 合肥德博生物能源科技有限公司 | A kind of device and method of biomass gasifying hydrogen making |
| CN111454752A (en) * | 2020-03-09 | 2020-07-28 | 深圳市松石环保科技有限公司 | Organic solid waste cracking and gasifying device |
| CN112480965A (en) * | 2020-11-20 | 2021-03-12 | 张俊霞 | Device and method for preparing biological hydrogen alkane and active carbon by adopting waste plastics and biomass |
| CN114806619A (en) * | 2022-04-28 | 2022-07-29 | 西安交通大学 | System and method for recycling all components of waste tire |
-
2012
- 2012-12-18 CN CN2012207021293U patent/CN203128183U/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103011157A (en) * | 2012-12-18 | 2013-04-03 | 北京神雾环境能源科技集团股份有限公司 | System and method for producing activated carbon and hydrogen through low-temperature pyrolysis of biomass steam |
| CN103011157B (en) * | 2012-12-18 | 2014-12-03 | 北京神雾环境能源科技集团股份有限公司 | System and method for producing activated carbon and hydrogen through low-temperature pyrolysis of biomass steam |
| CN106629710A (en) * | 2016-12-05 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | System and method for preparing activated carbon |
| CN106629715A (en) * | 2016-12-08 | 2017-05-10 | 北京神雾环境能源科技集团股份有限公司 | System and method for preparing active carbon by biomass |
| CN107416767A (en) * | 2017-08-16 | 2017-12-01 | 华中科技大学 | A kind of method that hydrogen and carbon electrode material are prepared using biomass |
| CN109852421A (en) * | 2019-02-25 | 2019-06-07 | 合肥德博生物能源科技有限公司 | A kind of device and method of biomass gasifying hydrogen making |
| CN111454752A (en) * | 2020-03-09 | 2020-07-28 | 深圳市松石环保科技有限公司 | Organic solid waste cracking and gasifying device |
| CN112480965A (en) * | 2020-11-20 | 2021-03-12 | 张俊霞 | Device and method for preparing biological hydrogen alkane and active carbon by adopting waste plastics and biomass |
| CN114806619A (en) * | 2022-04-28 | 2022-07-29 | 西安交通大学 | System and method for recycling all components of waste tire |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Patentee before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
|
| CP03 | Change of name, title or address | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: System for producing active carbon and hydrogen by biomass steam low-temperature pyrolysis Effective date of registration: 20180322 Granted publication date: 20130814 Pledgee: The Bank of Beijing Limited by Share Ltd. Anwar Road Branch Pledgor: Shenwu Technology Group Co.,Ltd. Registration number: 2018990000210 |
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| CF01 | Termination of patent right due to non-payment of annual fee |