CN104129754A - Biomass pyrolysis and chemical chain hydrogen production coupled continuous reaction device and method for producing hydrogen gas with biomass pyrolysis and chemical chain hydrogen production coupled continuous reaction device - Google Patents
Biomass pyrolysis and chemical chain hydrogen production coupled continuous reaction device and method for producing hydrogen gas with biomass pyrolysis and chemical chain hydrogen production coupled continuous reaction device Download PDFInfo
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- CN104129754A CN104129754A CN201410326789.XA CN201410326789A CN104129754A CN 104129754 A CN104129754 A CN 104129754A CN 201410326789 A CN201410326789 A CN 201410326789A CN 104129754 A CN104129754 A CN 104129754A
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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Abstract
The invention relates to a biomass pyrolysis and chemical chain hydrogen production coupled continuous reaction device and method for producing hydrogen gas with the device. The invention relates to the technical field of novel energy. According to the invention, a device with coupled components of a pyrolysis gasification device and a rotary chemical chain membrane hydrogen production device is adopted. The device is used for producing hydrogen gas. Raw materials are environment-friendly and renewable resources such as biomass and water vapour. No complicated separation and purification device is needed during a preparation process. Obtained hydrogen gas has relatively high purity, and does not contain tar. The device and the method provided by the invention has good market prospect and environment benefit.
Description
Technical field
The present invention relates to a kind of formation reaction device of clean energy and utilize this device to prepare the method for purified hydrogen, be specifically related to a kind of biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus and utilize this device to prepare the method for hydrogen.
Background technology
Hydrogen is a kind of desirable energy of clean and effective environmental protection, and along with hydrogen fuel cell is in succession on probation in world Ge great motor corporation, the range of application of Hydrogen Energy constantly expands.More than 90% hydrogen in the whole world comes from steam reforming or the partial oxidation of fossil oil at present, but the dust, the SO that produce in process of production
x, NO
xdeng causing serious environmental pollution.
Biomass are the abundant renewable resourcess in source, have the features such as reserves are large, carbon cycle.Research is at present found, utilizes biomass hydrogen preparation, can greatly reduce the secondary pollution that energy irrational utilization mode is brought, experimental result CO
2approach zero release, fundamentally solve fossil energy and utilize the problems such as the environmental pollution that brings in process and Greenhouse effect, for improving physical environment, promote that human kind sustainable development has important meaning.
Existing biomass hydrogen preparation technology can be divided into two classes, and a class be take biomass as raw material, by thermochemical method and technology hydrogen making, as biomass pyrogenation gasification hydrogen manufacturing, plasma gasification hydrogen manufacturing, supercritical water gasification hydrogen production etc.; Another kind of is to utilize biological approach reforming hydrogen manufacturing, as microorganism photodissociation hydrogen manufacturing, and ferment for hydrogen production and the two coupling etc.Thermochemistry hydrogen manufacturing and bio-transformation hydrogen manufacturing have different features and adaptability to raw material separately, recent domestic has all been carried out the wide research of sending out to above-mentioned several hydrogen production process, but in general, plasma gasification hydrogen manufacturing, supercritical water gasification hydrogen production energy consumption is excessive, Wood Adhesives from Biomass hydrogen manufacturing exists again fermentation condition harsh, Accumulation of Organic Acids in fermenting process, production capacity is difficult for the problems such as amplification, also need further further investigation, and biomass pyrogenation gasification hydrogen producing technology is fast with its thermal chemical reaction speed, production intensity is large, can realize from thermalization, the easy feature such as mass-producing and demonstrate wide application prospect.
The more biomass pyrogenation gasification hydrogen producing technology of current research is that biomass produce hydrogeneous fuel gas through gasification under gasifying medium participates in as air, water vapour, pure oxygen etc., through reformation, purification, separated, purification hydrogen making, gasifying reactor is generally fixed bed and fluidized-bed reactor again.Although this, first producing hydrogen purifies again, the technique of separating-purifying and technological line can be realized biomass pyrolytic hydrogen manufacturing, as turn S of Hawaii, America university etc. studies biomass fluid bed steam gasification hydrogen manufacturing under excess oxygen, obtain hydrogen output 128g/kg biomass, deduction rare gas element hydrogen is the highest consists of 57.4%, domestic Chinese Academy of Sciences Guangzhou Energy Research Institute, Chinese University of Science and Technology, the units such as Southeast China University are also from theoretical and experimentally this operational path is studied, confirmed its feasibility, but this technical scheme adds reformation because of need, purify, the links such as separating-purifying make complex process, energy consumption is higher, greatly raised hydrogen manufacturing cost, and hydrogen making purity is lower, tar content is relative also higher, and a kind of good biomass-making hydrogen production device can not only be realized biomass reforming hydrogen producing technology route, also should be taken into account the energy consumption of device, hydrogen manufacturing cost, hydrogen manufacturing purity, tar content and device operability etc.
Summary of the invention
The object of the invention is to overcome the shortcoming existing in existing biomass pyrogenation gasification device for producing hydrogen, design a kind of novel biomass pyrogenation gasification hydrogen making reaction device, to produce the hydrogen that purity is higher, do not need complicated purification separating technology, energy consumption is low, cost is few, and tar content is low, simple to operate, the biological carbon that hydrogen manufacturing produces can also be for improving edatope, repairing heavy metal in soil pollutes purposes such as (Pb, Cd), reaches the object of the high-efficiency cleaning conversion of biofuel.
Technical scheme of the present invention is as follows:
A biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus, this device comprises: for biomass pyrolytic being generated to the biomass pyrogenation gasification device of pyrolysis gas of biomass, for alternately there is with pyrolysis gas of biomass and water vapour the rotation chemical chain film reaction device for producing hydrogen that redox reaction is prepared hydrogen;
Described biomass pyrogenation gasification device comprises opening for feed, pyrolytic gasification reactor and pyrolysis gas output channel;
Described rotation chemical chain film reaction device for producing hydrogen is cylindrical shape, comprises heatproof housing, reactant gases diffuser, Rotary Oxygen carrier reactor and generates gas output device; Described Rotary Oxygen carrier reactor is by axis and can form around the oxygen carrier rotor of middle shaft rotation; Described oxygen carrier internal rotor is that cellular duct is provided with the oxygen carrier film of load lattice oxygen by the cellular duct structure at some gas passages interval, and described gas passage is parallel with axis; Described reactant gases diffuser and generation gas output device are separately positioned on the axial two ends of Rotary Oxygen carrier device for producing hydrogen axis; Described reactant gases diffuser is divided at least three fan-shaped air chambers by the air seal plate parallel with axis, is respectively pyrolysis gas inlet plenum, water vapour inlet plenum and air inlet chamber; Described generation gas output device is also divided at least three fan-shaped air chambers by the air seal plate parallel with axis, is respectively pyrolysis gas tail gas output chamber, hydrogen output chamber and air tail gas output chamber; Described pyrolysis gas inlet plenum is corresponding with the position of pyrolysis gas tail gas output chamber, and water vapour inlet plenum is corresponding with the position of hydrogen output chamber, and air inlet chamber is corresponding with the position of air tail gas output chamber;
Described pyrolysis gas output channel is communicated with pyrolysis gas inlet plenum.
Particularly, the pyrolysis gas inlet plenum of described reactant gases diffuser, water vapour inlet plenum and air inlet chamber, be also provided with rare gas element inlet plenum between two adjacent air chambers; Described generation gas output device pyrolysis gas tail gas output chamber, hydrogen output chamber and air tail gas output chamber, between two adjacent air chambers, the position part of corresponding described rare gas element inlet plenum is also provided with rare gas element output chamber.
Particularly, the material in the cellular duct of described oxygen carrier rotor is hydrotalcite structure material; The working temperature of oxygen carrier rotor is 800～1000 ℃, and cellular duct diameter is 2-6mm.
Particularly, described generation gas output device is also connected with condensation of gas collection device.
Particularly, the opening for feed of described biomass pyrogenation gasification device is connected with feeding screw.
Particularly, the bottom of described biomass pyrogenation gasification device is provided with ash exhauster.
Particularly, in the pyrolytic gasification reactor of described biomass pyrogenation gasification device, be provided with for separating the traverse baffle of solid materials and gas, described traverse baffle is divided into pyrolytic gasification reactor and the first chamber of feeding inlet and the second chamber communicating with pyrolysis gas output channel.
Particularly, the working temperature of described pyrolytic gasification reactor is 800～850 ℃.
The present invention also provides the method for utilizing described device to prepare hydrogen: (1) is placed in biomass pyrogenation gasification device by biomass, carries out pyrolysis at 800～850 ℃, generates and contains H
2, CO, CH
4, CO
2pyrolysis gas; Pyrolysis gas enters into pyrolysis gas inlet plenum by pyrolysis gas output channel, and enter into the oxygen carrier rotor corresponding with pyrolysis gas inlet plenum position, and there is redox reaction, the lattice oxygen of the oxygen carrier film in region is oxidized pyrolysis gas, generate tail gas, main component is CO
2and H
2o, lattice oxygen is reduced; (2) toward water vapour inlet plenum, pass into water vapour, air inlet chamber passes into air, and rare gas element inlet plenum passes into nitrogen; Keep the temperature of Rotary Oxygen carrier reactor at 800～1000 ℃; (3) start oxygen carrier rotor and make it around middle shaft rotation, make the region oxygen carrier film being reduced by pyrolysis gas successively by nitrogen-water vapor-nitrogen-air-nitrogen purging; The oxygen carrier film and the water vapor that by pyrolysis gas, are reduced react, and water vapor is reduced into hydrogen, and the oxygen carrier film being reduced is restored; Oxygen carrier film continues to react with air, guarantees oxygen carrier film load lattice oxygen again; The effect of nitrogen is that two interregional reactant gases and tail gas are separated thoroughly; (4) tail gas of pyrolysis gas enters pyrolysis gas tail gas output chamber; Hydrogen enters into hydrogen output chamber; Nitrogen enters rare gas element output chamber; Tail gas after air reaction enters into air tail gas output chamber; The various gases that generate discharge or collect after condensation; (5) oxygen carrier rotor constantly rotates, the hydrogen production process of above-mentioned (1)-(4) of circulating.
The present invention adopts biomass pyrogenation gasification and hydrogen production of chemical chain coupling continuous reaction apparatus, compared with prior art, advantage of the present invention and innovative point are: 1) adopt biomass pyrolytic and hydrogen production of chemical chain coupling continuous system to prepare H2, without complicated gas delivery purification system, cost is low, simple to operate.2) under oxygen carrier high temperature, tar is had to catalytic pyrolysis effect, can reduce the coal-tar middle oil content of product.3) the Rotary Oxygen vector rotor of cellular duct structure, does not need the circulation of driving bed material, long service life, and energy consumption is little, can guarantee the operation of lasting and isothermal simultaneously.4) the oxygen carrier rotor in cellular duct has heat accumulation function, can directly water vapour hydrogen manufacturing district and air reaction district partial reaction heat be passed to fuel reaction district, reduces energy consumption.5) biological carbon that biomass pyrolysis system produces can be for improving the fields such as edatope, the heavy metal contamination of rehabilitating soil.Once there is wide market outlook and environmental benefit after the present invention applies.
Accompanying drawing explanation
Fig. 1 is the embodiment of the present invention 1 biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus schematic diagram;
Fig. 2 is the face upwarding section of the embodiment of the present invention 1 rotation chemical chain film reaction device for producing hydrogen;
Fig. 3 is the schematic perspective view of the embodiment of the present invention 1 rotation chemical chain film reaction device for producing hydrogen;
Reference numeral: I-biomass pyrogenation gasification device; II-rotation chemical chain film reaction device for producing hydrogen;
1-opening for feed; 2-feeding screw; 3-pyrolytic gasification reactor; 31-the first chamber; 32-the second chamber; 4-traverse baffle; 5-ash exhauster; 6-pyrolysis gas output channel; 7-heatproof housing; 8-Rotary Oxygen carrier reactor; 81-axis; 82-oxygen carrier rotor; The cellular duct of 821-; 822-gas passage; 9-reactant gases diffuser; 91-pyrolysis gas inlet plenum; 92-water vapour inlet plenum; 93-air inlet chamber; 94,95,96-rare gas element inlet plenum; 10-and generation gas output device; 101-pyrolysis gas output chamber; 102-water vapour output chamber; 103-air output chamber; 104,105,106-rare gas element output chamber; 11-condensation of gas device; 12-air seal plate.
Embodiment
Below in conjunction with drawings and Examples, the present invention will be further described, and embodiment is not in order to limit the scope of the claims of the present invention, and the equivalence that all the present invention of disengaging do is implemented or change, all should be contained in this patent protection domain.
Embodiment 1:
Biomass pyrolytic and a hydrogen production of chemical chain coupling continuous reaction apparatus, as shown in Figure 1, this system is comprised of two portions, biomass pyrogenation gasification device and rotation chemical chain film reaction device for producing hydrogen.
Biomass pyrogenation gasification device comprises opening for feed 1, pyrolytic gasification reactor 3, the pyrolysis gas output channel 6 connecting successively; Opening for feed 1 connects feeding screw 2; In pyrolytic gasification reactor 3, be provided with for separating the traverse baffle 4 of solid materials and gas, traverse baffle 4 is separated into the first chamber 31 and the second chamber 32 by pyrolytic gasification reactor 3, opening for feed 1 communicates with the first chamber 31, and the second chamber 32 communicates with pyrolysis gas output channel 6; Bottom at pyrolytic gasification reactor 3 is also provided with ash exhauster 5.The diameter 80mm of pyrolytic gasification reactor 3, high 1000mm, made by high temperature resistant stainless steel material (904L), has hearth-type heating system that heat is provided.
In conjunction with Fig. 2 and Fig. 3, rotation chemical chain film reaction device for producing hydrogen is cylindrical shape, comprises heatproof housing 7, reactant gases diffuser 9, Rotary Oxygen carrier reactor 8 and generation gas output device 10.Heatproof housing 7 is made by high temperature resistant stainless steel material (904L), and Rotary Oxygen carrier reactor 8 provides heat by hearth-type heating system.
Rotary Oxygen carrier reactor 8 comprises that axis 81 and the oxygen carrier rotor 82 that can rotate around axis 81 form, and oxygen carrier rotor 82 inside are that cellular duct 821 is provided with the oxygen carrier film of load lattice oxygen by cellular duct 821 structures at gas passage 822 intervals.Oxygen carrier rotor 82 is the cylindrical of diameter 1000mm, high 1600mm, the NiFe that material is hydrotalcite structure
2o
4, described hydrotalcite structure material can also be selected from one or more pure metal or the oxide compound etc. in Ni, Fe, Sr, Cu, and cellular duct diameter is 3mm.Gas passage 822 is parallel with axis 81.
Reactant gases diffuser 9 is placed in the bottom of Rotary Oxygen carrier reactor 8, by some blocks of air seal plates 12, along central axis direction, be divided into six air chambers, comprise pyrolysis gas inlet plenum 91, water vapour inlet plenum 92, air inlet chamber 93, and the rare gas element inlet plenum 94,95,96 between these three air chambers are adjacent between two.
Generate the top that gas output device 10 is placed in Rotary Oxygen carrier reactor 8, also by some blocks of air seal plates, along central axis direction, be divided into six air chambers, for pyrolysis gas tail gas output chamber 101, hydrogen output chamber 102, air tail gas output chamber 103, and the output of the rare gas element between these three air chambers are adjacent between two chamber 104,105,106.
Pyrolysis gas inlet plenum 91 is corresponding with the position of pyrolysis gas tail gas output chamber 101, and water vapour inlet plenum 92 is corresponding with the position of hydrogen output chamber 102, and air inlet chamber 93 is corresponding with the position of air tail gas output chamber 103; Rare gas element inlet plenum 94,95,96 is corresponding with the position of rare gas element output chamber 104,105,106 respectively.
Described pyrolysis gas output channel 6 is communicated with pyrolysis gas inlet plenum 91.
Generating gas output device 10 is also connected with condensation of gas device 11.
Embodiment 2
Utilize biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare the method for hydrogen: biomass enter pyrolytic gasification reactor 3 under the promotion of feeding screw 2, carry out pyrolytic gasification at 800 ℃, mainly generate H
2, CO, CH
4, CO
2deng pyrolysis gas.Pyrolysis gas guides laggard the second chamber 32 through traverse baffle 4, and enters pyrolysis gas inlet plenum 91 by entering pyrolysis gas output channel 6.The biomass lime-ash reacting completely is got rid of reactor through ash exhauster 5.
Water vapour is introduced into water vapour inlet plenum 92, and nitrogen is introduced into rare gas element inlet plenum 94,95,96, and air is introduced into air inlet chamber 93.Keeping the temperature of Rotary Oxygen carrier reactor 8 is 1000 ℃, and oxygen carrier rotor 82 rotates around axis 91 under the drive of motor.Oxygen carrier 821 in oxygen carrier rotor 82 and duct are successively by pyrolysis gas-nitrogen-water vapour-nitrogen-air purge.Oxygen carrier first generates CO by pyrolysis gas oxidation
2and H
2o tail gas, oxygen carrier is reduced, and pyrolysis gas also carries out thermal exchange with oxygen carrier, and tail gas is discharged through pyrolysis gas tail gas output chamber 101; The oxygen carrier then with reductibility reacts with water vapour, and high-temperature vapor is H at oxygen carrier film Surface disintegration
2recover the lattice oxygen of oxygen carrier film with active oxygen atom, the collecting through hydrogen output chamber 102 of generation; The last further oxidation by air of oxygen carrier film, is restored the lattice oxygen in oxygen carrier film completely, and the tail gas of generation is discharged through air tail gas output chamber 103; In oxygen carrier rotor rotation process, before contacting, first through nitrogen purging, guarantee can not mix generation side reaction between reactant gases with front and back two reactant gasess, nitrogen is finally discharged through rare gas element take-off equipment 103,104,105.
Biomass pyrolysis reactor working temperature is 800-850 ℃, and hydrogen production of chemical chain reactor working temperature is 800-1000 ℃; Installing raw materials used can be the biomass materials such as stalk, wood chip, rice husk, bagasse, and the pine powder of take in the present embodiment is tested as representative, feeding rate 5kg/h; The biological flue gas generating (flow is 60L/min) and air (60L/min), water vapour (flow 50L/min, 120 ℃), rare gas element (N2,50L/min), generate tail gas through exporting 19 outflows, after condensation, approximately 3～5min once sampling, analyzes by gas-chromatography, and result is as follows:
Table 1 utilizes material pyrolysis and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare condition and the result of hydrogen
Embodiment 3:
Utilize the equipment of embodiment 1, according to the technical process of executing example 2, by the implementation condition of table 2, prepare hydrogen, and analyze generating gas by gas-chromatography, result is as follows:
Table 2 utilizes material pyrolysis and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare condition and the result of hydrogen
Embodiment 4:
Utilize the equipment of embodiment 1, according to the technical process of executing example 2, by the implementation condition of table 3, prepare hydrogen, and analyze generating gas by gas-chromatography, result is as follows:
Table 3 utilizes material pyrolysis and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare condition and the result of hydrogen
Embodiment 5:
Utilize the equipment of embodiment 1, according to the technical process of executing example 2, by the implementation condition of table 4, prepare hydrogen, and analyze generating gas by gas-chromatography, result is as follows:
Table 4 utilizes material pyrolysis and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare condition and the result of hydrogen
Embodiment 6:
Utilize the equipment of embodiment 1, adopting the cellular duct of oxygen carrier diameter is 2mm, according to the technical process of executing example 2, by the implementation condition of table 5, prepares hydrogen, and analyzes generating gas by gas-chromatography, and result is as follows:
Table 5 utilizes material pyrolysis and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare condition and the result of hydrogen
Embodiment 7:
Utilize the equipment of embodiment 1, adopting the cellular duct of oxygen carrier diameter is 6mm, according to the technical process of executing example 2, by the implementation condition of table 6, prepares hydrogen, and analyzes generating gas by gas-chromatography, and result is as follows:
Table 6 utilizes material pyrolysis and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare condition and the result of hydrogen
Claims (9)
1. a biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus, is characterized in that this device comprises: for biomass pyrolytic being generated to the biomass pyrogenation gasification device of pyrolysis gas of biomass, for alternately there is with pyrolysis gas of biomass and water vapour the rotation chemical chain film reaction device for producing hydrogen that redox reaction is prepared hydrogen;
Described biomass pyrogenation gasification device comprises opening for feed (1), pyrolytic gasification reactor (3) and pyrolysis gas output channel (6);
Described rotation chemical chain film reaction device for producing hydrogen is cylindrical shape, comprises heatproof housing (7), reactant gases diffuser (9), Rotary Oxygen carrier reactor (8) and generates gas output device (10); Described Rotary Oxygen carrier reactor (8) is by axis (81) and can form around the oxygen carrier rotor (82) of middle shaft rotation; Described oxygen carrier rotor (82) inside is cellular duct (821) structure by some gas passages (822) interval, cellular duct (821) is provided with the oxygen carrier film of load lattice oxygen, described gas passage (822) parallel with axis (81); Described reactant gases diffuser (9) and generation gas output device (10) are separately positioned on the axial two ends of Rotary Oxygen carrier device for producing hydrogen (8) axis; Described reactant gases diffuser (9) is divided at least three fan-shaped air chambers by the air seal plate (12) parallel with axis, is respectively pyrolysis gas inlet plenum (91), water vapour inlet plenum (92) and air inlet chamber (93); Described generation gas output device (10) is also divided at least three fan-shaped air chambers by the air seal plate parallel with axis, is respectively pyrolysis gas tail gas output chamber (101), hydrogen output chamber (102) and air tail gas output chamber (103); Described pyrolysis gas inlet plenum (91) is corresponding with the position of pyrolysis gas tail gas output chamber (101), water vapour inlet plenum (92) is corresponding with the position of hydrogen output chamber (102), and air inlet chamber (93) is corresponding with the position of air tail gas output chamber (103); Described pyrolysis gas output channel (6) is communicated with pyrolysis gas inlet plenum (91).
2. device as claimed in claim 1, is characterized in that, between two adjacent air chambers of described reactant gases diffuser (9), is also provided with rare gas element inlet plenum; Between two adjacent air chambers of described generation gas output device (10), the position part of corresponding described rare gas element inlet plenum is also provided with rare gas element output chamber.
3. install as claimed in claim 1, it is characterized in that, the material in the cellular duct of described oxygen carrier rotor is hydrotalcite structure material; The working temperature of oxygen carrier rotor is 800～1000 ℃, and cellular duct diameter is 2-6mm.
4. device as claimed in claim 1, is characterized in that, described generation gas output device (10) is also connected with condensation of gas collection device.
5. device as claimed in claim 1, is characterized in that, the opening for feed of described biomass pyrogenation gasification device (1) is connected with feeding screw.
6. device as claimed in claim 1, is characterized in that, the bottom of described biomass pyrogenation gasification device is provided with ash exhauster.
7. device as claimed in claim 1, it is characterized in that, in the pyrolytic gasification reactor (3) of described biomass pyrogenation gasification device, be provided with for separating the traverse baffle of solid materials and gas, described traverse baffle is divided into the first chamber communicating with opening for feed (1) and the second chamber communicating with pyrolysis gas output channel (6) by pyrolytic gasification reactor.
8. device as claimed in claim 1, is characterized in that, the working temperature of described pyrolytic gasification reactor is 800～850 ℃.
9. the method for utilizing biomass pyrolytic described in claim 1-8 any one and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare hydrogen, is characterized in that:
(1) biomass are placed in to biomass pyrogenation gasification device, carry out pyrolysis at 800～850 ℃, generate and contain H
2, CO, CH
4, CO
2pyrolysis gas; Pyrolysis gas enters into pyrolysis gas inlet plenum by pyrolysis gas output channel, and enter into the oxygen carrier rotor corresponding with pyrolysis gas inlet plenum position, and there is redox reaction, the lattice oxygen of the oxygen carrier film in region is oxidized pyrolysis gas, generate tail gas, lattice oxygen is reduced;
(2) toward water vapour inlet plenum, pass into water vapour, air inlet chamber passes into air, and rare gas element inlet plenum passes into nitrogen; Keep the temperature of Rotary Oxygen carrier reactor at 800～1000 ℃;
(3) start oxygen carrier rotor and make it around middle shaft rotation, make the region oxygen carrier film being reduced by pyrolysis gas successively by nitrogen-water vapor-nitrogen-air-nitrogen purging; The oxygen carrier film and the water vapor that by pyrolysis gas, are reduced react, and water vapor is reduced into hydrogen, and the oxygen carrier film being reduced is restored; Oxygen carrier film continues to react with air, guarantees oxygen carrier film load lattice oxygen again; The effect of nitrogen is that two interregional reactant gases and tail gas are separated thoroughly;
(4) tail gas of pyrolysis gas enters pyrolysis gas tail gas output chamber; Hydrogen enters into hydrogen output chamber; Nitrogen enters rare gas element output chamber; Tail gas after air reaction enters into air tail gas output chamber; The various gases that generate discharge or collect after condensation;
(5) oxygen carrier rotor constantly rotates, the hydrogen production process of above-mentioned (1)-(4) of circulating.
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| CN108869796A (en) * | 2018-06-15 | 2018-11-23 | 上海理工大学 | A kind of rotation combination valve and method for fixed bed hydrogen production of chemical chain |
| CN112645282A (en) * | 2020-12-10 | 2021-04-13 | 广东醇氢新能源研究院有限公司 | Hydrogen production device |
| CN112723308A (en) * | 2021-01-18 | 2021-04-30 | 浙江华电器材检测研究所有限公司 | Method for preparing hydrogen by catalyzing chain with carbon hydrocarbon fuel plasma |
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