CN104129754B - 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 - Google Patents
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 Download PDFInfo
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- CN104129754B CN104129754B CN201410326789.XA CN201410326789A CN104129754B CN 104129754 B CN104129754 B CN 104129754B CN 201410326789 A CN201410326789 A CN 201410326789A CN 104129754 B CN104129754 B CN 104129754B
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- 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
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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 present invention relates 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, belonging to technical field of new energies.The present invention adopts pyrolysis gasifying device and rotates the device of chemical chain film device for producing hydrogen coupling, this device is utilized to prepare hydrogen, raw material adopts the environmental protection such as biomass, water vapour renewable resources, isolation andpurification device that need not be complicated in preparation process, the hydrogen purity prepared is higher, and not containing tar.The present invention has wide market outlook and environmental 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 tried out in succession in Ge great motor corporation of the world, the range of application of Hydrogen Energy constantly expands.The current hydrogen of global more than 90% comes from steam reforming or the partial oxidation of fossil oil, but the dust produced in process of production, SO
x, NO
xetc. causing serious environmental pollution.
Biomass are renewable resourcess of abundance, have the features such as reserves are large, carbon cycle.Current research finds, utilizes biomass hydrogen preparation, can greatly reduce the secondary pollution that energy irrational utilization mode is brought, experimental result CO
2close to zero release, fundamentally solving fossil energy and utilize the problems such as the environmental pollution that brings in process and Greenhouse effect, for improving physical environment, promoting that human kind sustainable development has important meaning.
Existing biomass hydrogen preparation technology can be divided into two classes, and a class 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 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 carried out the wide research sent out to above-mentioned several hydrogen production process, but in general, plasma gasification hydrogen manufacturing, supercritical water gasification hydrogen production energy consumption is excessive, there is again fermentation condition harshness in Wood Adhesives from Biomass hydrogen manufacturing, Accumulation of Organic Acids in fermenting process, production capacity such as not easily to amplify at the problem, 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, features such as easy mass-producing and demonstrate wide application prospect.
The more biomass pyrogenation gasification hydrogen producing technology of current research be biomass gasifying medium as air, water vapour, pure oxygen etc. participate under produce hydrogeneous fuel gas through gasification, again through reformation, purification, separation, purification hydrogen making, gasifying reactor is generally fixed bed and fluidized-bed reactor.First produce hydrogen although this to purify again, the technique of separating-purifying and technological line can realize biomass pyrolytic hydrogen manufacturing, as Hawaii, America university turnS 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 be experimentally studied this operational path, confirm its feasibility, but this technical scheme is because adding reformation, purification, the links such as separating-purifying make complex process, energy consumption is higher, greatly raise 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 realize 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 existed in existing biomass pyrogenation gasification device for producing hydrogen, design a kind of novel biomass pyrogenation gasification hydrogen making reaction device, to produce the higher hydrogen of purity, do not need complicated purification & isolation technique, 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 used for improving edatope, repairing heavy metal in soil pollutes purposes such as (Pb, Cd), the object that the high-efficiency cleaning reaching biofuel transforms.
Technical scheme of the present invention is as follows:
A kind of biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus, this device comprises: for biomass pyrolytic is generated pyrolysis gas of biomass biomass pyrogenation gasification device, be used for alternately occurring with pyrolysis gas of biomass and water vapour the rotation chemical chain film reaction device for producing hydrogen that redox reaction prepares 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 by the cellular pore passage structure at some gas passage intervals, and cellular duct is provided with the oxygen carrier film of load lattice oxygen, and described gas passage is parallel with axis; Described reactant gases diffuser and generation gas output device are separately positioned on the two ends of Rotary Oxygen carrier reactor axis 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 that pyrolysis gas tail gas exports room, hydrogen exports room and air tail gas exports room; Described pyrolysis gas inlet plenum is corresponding with the position that pyrolysis gas tail gas exports room, and water vapour inlet plenum is corresponding with the position that hydrogen exports room, and air inlet chamber is corresponding with the position that air tail gas exports room;
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 cells; Described generation gas output device pyrolysis gas tail gas exports room, hydrogen exports room and air tail gas exports room, and between two adjacent air cells, the position part of corresponding described rare gas element inlet plenum is also provided with rare gas element and exports room.
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 DEG C, and cellular channel 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, be provided with the traverse baffle for separating solid materials and gas in the pyrolytic gasification reactor of described biomass pyrogenation gasification device, pyrolytic gasification reactor is divided into the first chamber communicated with opening for feed and the second chamber communicated with pyrolysis gas output channel by described traverse baffle.
Particularly, the working temperature of described pyrolytic gasification reactor is 800 ~ 850 DEG C.
Present invention also offers the method utilizing described device to prepare hydrogen: biomass are placed in biomass pyrogenation gasification device by (1), at 800 ~ 850 DEG C, carry out pyrolysis, generate containing H
2, CO, CH
4, CO
2pyrolysis gas; Pyrolysis gas enters into pyrolysis gas inlet plenum by pyrolysis gas output channel, and entering into the oxygen carrier rotor corresponding with pyrolysis gas inlet plenum position, redox reaction occurs, and pyrolysis gas is oxidized by the lattice oxygen of the oxygen carrier film in region, generate tail gas, main component is CO
2and H
2o, lattice oxygen is reduced; (2) pass into water vapour toward water vapour inlet plenum, 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 DEG C; (3) starting oxygen carrier rotor makes it around middle shaft rotation, and the region oxygen carrier film by pyrolysis gas reduces is purged by nitrogen-water vapor-nitrogen-air-nitrogen successively; The oxygen carrier film reduced by pyrolysis gas and water vapor react, and water vapor is reduced into hydrogen, and the oxygen carrier film be reduced is restored; Oxygen carrier film continues to react with air, ensures oxygen carrier film load lattice oxygen again; The effect of nitrogen is that two interregional reactant gasess and tail gas are separated thoroughly; (4) tail gas of pyrolysis gas enters pyrolysis gas tail gas and exports room; Hydrogen enters into hydrogen and exports room; Nitrogen enters rare gas element and exports room; Tail gas after air reaction enters into air tail gas and exports room; The various gases generated discharge or collect after condensation; (5) oxygen carrier rotor constantly rotates, the hydrogen production process of above-mentioned (1)-(4) of namely 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 the need to the gas delivery purification system of complexity, cost is low, simple to operate.2) to tar, there is catalytic pyrolysis effect under oxygen carrier high temperature, the coal-tar middle oil content of product can be reduced.3) the Rotary Oxygen vector rotor of cellular pore passage structure, do not need to drive the circulation of bed material, long service life, energy consumption is little, can guarantee to continue the operation with isothermal simultaneously.4) the oxygen carrier rotor in cellular duct has heat accumulation function, can directly by water vapour hydrogen manufacturing district and air reaction district partial reaction heat trnasfer to fuel reaction district, reduce energy consumption.5) biological carbon that biomass pyrolysis system produces may be used for improving edatope, the fields such as the heavy metal contamination of rehabilitating soil.The present invention is once have wide market outlook and environmental benefit after applying.
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 that the embodiment of the present invention 1 rotates chemical chain film reaction device for producing hydrogen;
Fig. 3 is the schematic perspective view that the embodiment of the present invention 1 rotates chemical chain film reaction device for producing hydrogen;
Reference numeral: I-biomass pyrogenation gasification device; II-rotate chemical chain film reaction device for producing hydrogen;
1-opening for feed; 2-feeding screw; 3-pyrolytic gasification reactor; 31-first chamber; 32-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-generates gas output device; 101-pyrolysis gas tail gas exports room; 102-hydrogen exports room; 103-air tail gas exports room; 104,105,106-rare gas element exports room; 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 also not used 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 changed, and all should be contained in this patent protection domain.
Embodiment 1:
A kind of biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus, as shown in Figure 1, this system is made up of two portions, biomass pyrogenation gasification device and rotation chemical chain film reaction device for producing hydrogen.
Biomass pyrogenation gasification device comprises the opening for feed 1, pyrolytic gasification reactor 3, the pyrolysis gas output channel 6 that connect successively; Opening for feed 1 connects feeding screw 2; The traverse baffle 4 for separating solid materials and gas is provided with in pyrolytic gasification reactor 3, pyrolytic gasification reactor 3 is separated into the first chamber 31 and the second chamber 32 by traverse baffle 4, opening for feed 1 communicates with the first chamber 31, and the second chamber 32 communicates with pyrolysis gas output channel 6; Ash exhauster 5 is also provided with in the bottom of pyrolytic gasification reactor 3.The diameter 80mm of pyrolytic gasification reactor 3, high 1000mm, be made up of high temperature resistant stainless steel material (904L), has hearth-type heating system to provide heat.
Composition graphs 2 and Fig. 3, rotating 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 up of 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 axis 81 and can form around the oxygen carrier rotor 82 of axis 81 rotation, and oxygen carrier rotor 82 inside is that cellular duct 821 is provided with the oxygen carrier film of load lattice oxygen by cellular duct 821 structure at gas passage 822 interval.Oxygen carrier rotor 82 be diameter 1000mm, high 1600mm cylindrical, material is the NiFe of hydrotalcite structure
2o
4, described hydrotalcite structure material can also be selected from the pure metal of one or more or oxide compound etc. in Ni, Fe, Sr, Cu, and cellular channel 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, six air chambers are divided into along central axis direction by some blocks of air seal plates 12, 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 six air chambers are divided into by some blocks of air seal plates along central axis direction, for pyrolysis gas tail gas exports room 101, hydrogen output room 102, air tail gas output room 103, and the rare gas element between these three air chambers are adjacent between two exports room 104,105,106.
Pyrolysis gas inlet plenum 91 is corresponding with the position that pyrolysis gas tail gas exports room 101, and water vapour inlet plenum 92 is corresponding with the position that hydrogen exports room 102, and air inlet chamber 93 is corresponding with the position that air tail gas exports room 103; Rare gas element inlet plenum 94,95,96 exports room 104,105,106 respectively position with rare gas element is corresponding.
Described pyrolysis gas output channel 6 is communicated with pyrolysis gas inlet plenum 91.
Generate gas output device 10 to be also connected with condensation of gas device 11.
Embodiment 2
Biomass pyrolytic and hydrogen production of chemical chain coupling continuous reaction apparatus is utilized to prepare the method for hydrogen: biomass enter pyrolytic gasification reactor 3 under the promotion of feeding screw 2, carry out pyrolytic gasification, mainly generate H at 800 DEG C
2, CO, CH
4, CO
2deng pyrolysis gas.Pyrolysis gas guides laggard second chamber 32 through traverse baffle 4, and passes through to enter pyrolysis gas inlet plenum 91 into pyrolysis gas output channel 6.The biomass lime-ash reacted completely gets 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.The temperature keeping Rotary Oxygen carrier reactor 8 is 1000 DEG C, and oxygen carrier rotor 82 rotates around axis 81 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.Pyrolysis gas oxidation is first generated CO by oxygen carrier
2and H
2o tail gas, oxygen carrier is reduced, and pyrolysis gas also carries out thermal exchange with oxygen carrier, and tail gas exports room 101 through pyrolysis gas tail gas and discharges; Oxygen carrier and the water vapour then with reductibility react, and high-temperature vapor is H at oxygen carrier film Surface disintegration
2the lattice oxygen of oxygen carrier film is recovered, collecting through hydrogen output room 102 of generation with active oxygen atom; The further oxidation by air of last oxygen carrier film, makes the lattice oxygen in oxygen carrier film be restored completely, and the tail gas of generation exports room 103 through air tail gas and discharges; In oxygen carrier rotor rotation process, first through nitrogen purging before contacting with front and back two reactant gases, ensure can not mix generation side reaction between reactant gases, nitrogen is finally discharged through rare gas element take-off equipment 103,104,105.
Biomass pyrolysis reactor working temperature is 800-850 DEG C, and hydrogen production of chemical chain reactor working temperature is 800-1000 DEG C; Device is raw materials used can be the biomass materials such as stalk, wood chip, rice husk, bagasse, is that representative is tested in the present embodiment with pine powder, feeding rate 5kg/h; The biological flue gas (flow is 60L/min) generated and air (60L/min), water vapour (flow 50L/min, 120 DEG C), rare gas element (N2,50L/min), generate tail gas through exporting 19 outflows, after condensation, sampling should be carried out for about 3 ~ 5min, analyzed 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 executing example 2, prepare hydrogen by the implementation condition of table 2, and analyzed generation 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 executing example 2, prepare hydrogen by the implementation condition of table 3, and analyzed generation 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 executing example 2, prepare hydrogen by the implementation condition of table 4, and analyzed generation 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, adopt the cellular channel diameter of oxygen carrier to be 2mm, according to the technical process executing example 2, prepare hydrogen by the implementation condition of table 5, and analyzed generation gas by gas-chromatography, 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, adopt the cellular channel diameter of oxygen carrier to be 6mm, according to the technical process executing example 2, prepare hydrogen by the implementation condition of table 6, and analyzed generation gas by gas-chromatography, 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. biomass pyrolytic and a hydrogen production of chemical chain coupling continuous reaction apparatus, is characterized in that this device comprises: for biomass pyrolytic is generated pyrolysis gas of biomass biomass pyrogenation gasification device, be used for alternately occurring with pyrolysis gas of biomass and water vapour the rotation chemical chain film reaction device for producing hydrogen that redox reaction prepares 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 by cellular duct (821) structure at some gas passages (822) interval, cellular duct (821) is provided with the oxygen carrier film of load lattice oxygen, and described gas passage (822) is parallel with axis (81); Described reactant gases diffuser (9) and generation gas output device (10) are separately positioned on the two ends of Rotary Oxygen carrier reactor (8) axis 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 that pyrolysis gas tail gas exports room (101), hydrogen exports room (102) and air tail gas output room (103); Described pyrolysis gas inlet plenum (91) is corresponding with the position that pyrolysis gas tail gas exports room (101), the position that water vapour inlet plenum (92) and hydrogen export room (102) is corresponding, and air inlet chamber (93) is corresponding with the position that air tail gas exports room (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, be also provided with rare gas element inlet plenum between two adjacent air cells of described reactant gases diffuser (9); Between two adjacent air cells 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 and exports room.
3. device 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 DEG C, and cellular channel diameter is 2-6mm.
4. device as claimed in claim 1, it 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, it is characterized in that, the opening for feed (1) of described biomass pyrogenation gasification device is connected with feeding screw.
6. device as claimed in claim 1, it 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, be provided with the traverse baffle for separating solid materials and gas in the pyrolytic gasification reactor (3) of described biomass pyrogenation gasification device, pyrolytic gasification reactor is divided into the first chamber communicated with opening for feed (1) and the second chamber communicated with pyrolysis gas output channel (6) by described traverse baffle.
8. device as claimed in claim 1, it is characterized in that, the working temperature of described pyrolytic gasification reactor is 800 ~ 850 DEG C.
9. utilize the biomass pyrolytic described in claim 2 and hydrogen production of chemical chain coupling continuous reaction apparatus to prepare the method for hydrogen, it is characterized in that:
(1) biomass are placed in biomass pyrogenation gasification device, at 800 ~ 850 DEG C, carry out pyrolysis, generate containing H
2, CO, CH
4, CO
2pyrolysis gas; Pyrolysis gas enters into pyrolysis gas inlet plenum by pyrolysis gas output channel, and entering into the oxygen carrier rotor corresponding with pyrolysis gas inlet plenum position, redox reaction occurs, and pyrolysis gas is oxidized by the lattice oxygen of the oxygen carrier film in region, generate tail gas, lattice oxygen is reduced;
(2) pass into water vapour toward water vapour inlet plenum, 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 DEG C;
(3) starting oxygen carrier rotor makes it around middle shaft rotation, and the region oxygen carrier film by pyrolysis gas reduces is purged by nitrogen-water vapor-nitrogen-air-nitrogen successively; The oxygen carrier film reduced by pyrolysis gas and water vapor react, and water vapor is reduced into hydrogen, and the oxygen carrier film be reduced is restored; Oxygen carrier film continues to react with air, ensures oxygen carrier film load lattice oxygen again; The effect of nitrogen makes two interregional reactant gasess and tail gas separate thoroughly;
(4) tail gas of pyrolysis gas enters pyrolysis gas tail gas and exports room; Hydrogen enters into hydrogen and exports room; Nitrogen enters rare gas element and exports room; Tail gas after air reaction enters into air tail gas and exports room; The various gases generated discharge or collect after condensation;
(5) oxygen carrier rotor constantly rotates, the hydrogen production process of above-mentioned (1)-(4) of namely circulating.
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| CN115948172B (en) * | 2022-12-29 | 2024-04-09 | 中国科学院广州能源研究所 | Device and method for preparing clean synthetic gas by organic solid waste pyrolysis-chemical chain reforming |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201501787U (en) * | 2009-09-14 | 2010-06-09 | 昆明理工大学 | Device utilizing lattice oxygen to partially oxidize natural gas to prepare synthetic gas |
| CN102198934A (en) * | 2011-04-20 | 2011-09-28 | 中国科学院广州能源研究所 | Method and device for producing hydrogen by using chemical chain |
| CN102515096A (en) * | 2011-11-22 | 2012-06-27 | 中国科学院广州能源研究所 | Application of three-dimensional ordered macro-porous perovskite type oxide in preparing hydrogen through carbonic fuel chemical chain |
| CN103204464A (en) * | 2013-03-29 | 2013-07-17 | 中国科学院广州能源研究所 | Cellular oxygen carrier chemical-looping reforming reactor |
-
2014
- 2014-07-09 CN CN201410326789.XA patent/CN104129754B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201501787U (en) * | 2009-09-14 | 2010-06-09 | 昆明理工大学 | Device utilizing lattice oxygen to partially oxidize natural gas to prepare synthetic gas |
| CN102198934A (en) * | 2011-04-20 | 2011-09-28 | 中国科学院广州能源研究所 | Method and device for producing hydrogen by using chemical chain |
| CN102515096A (en) * | 2011-11-22 | 2012-06-27 | 中国科学院广州能源研究所 | Application of three-dimensional ordered macro-porous perovskite type oxide in preparing hydrogen through carbonic fuel chemical chain |
| CN103204464A (en) * | 2013-03-29 | 2013-07-17 | 中国科学院广州能源研究所 | Cellular oxygen carrier chemical-looping reforming reactor |
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