CN209872347U - Device for preparing hydrogen by double fluidized bed biomass pyrolysis gasification - Google Patents

Device for preparing hydrogen by double fluidized bed biomass pyrolysis gasification Download PDF

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Publication number
CN209872347U
CN209872347U CN201920233990.1U CN201920233990U CN209872347U CN 209872347 U CN209872347 U CN 209872347U CN 201920233990 U CN201920233990 U CN 201920233990U CN 209872347 U CN209872347 U CN 209872347U
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pyrolysis
furnace
pyrolysis furnace
fluidized bed
absorbent
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张守军
王勤辉
蒋剑春
李益瑞
张守峰
吴银龙
赵成武
鲁万宝
冯干
宋俊阳
胡鹏
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Hefei Debo Bioenergy Science & Technology Co Ltd
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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 utility model provides a device of double fluidized bed living beings pyrolysis gasification preparation hydrogen, include: dual fluidizationThe bed comprises a fluidized bed pyrolysis furnace and a fluidized bed combustion furnace, the fluidized bed pyrolysis furnace comprises a pyrolysis furnace riser, the rear end of the pyrolysis furnace riser is connected with a pyrolysis furnace cyclone separator, the upper part of the pyrolysis furnace cyclone separator is connected with a shift reactor, the lower part of the pyrolysis furnace cyclone separator is connected with a pyrolysis furnace material returning valve, the other outlet of the pyrolysis furnace material returning valve is connected with the fluidized bed combustion furnace, and the fluidized bed combustion furnace comprises a combustion furnace riser; the other outlet of the return valve of the pyrolysis furnace is connected with the bottom of the lifting pipe of the combustion furnace; an oxygen carrier cyclone separator is arranged in the middle of a combustion furnace lifting pipe, and CO is arranged at the top of the combustion furnace lifting pipe2An absorbent cyclone; the utility model discloses need not the pure oxygen as the gasification agent in the preparation process, the system only needs the supplementary air can satisfy the production demand as gasification, low in production cost is honest and clean, and the pyrolysis oven does not use the air to fluidize, and the effective component content in its living beings gas is high.

Description

Device for preparing hydrogen by double fluidized bed biomass pyrolysis gasification
Technical Field
The utility model relates to a living beings utilize technical field, specifically are a device of double fluidized bed living beings pyrolysis gasification preparation hydrogen.
Background
With the development and utilization of new energy, hydrogen energy is gradually used by various industries due to its characteristics of safety, environmental protection, high energy and the like. The current common hydrogen production mode is as follows: the hydrogen is produced by electrolyzing water, fossil energy or other intermediate process gas, and because hydrogen energy is secondary energy, common hydrogen production modes still rely on traditional energy sources, such as: petroleum, coal (electrodes for electrolysis processes, coal to hydrogen, etc.) or electrical energy (since the main source of global electrical energy remains fossil energy conversion).
The biomass resource is taken as a renewable energy source with huge reserves, and is changed into high-efficiency clean energy such as hydrogen energy and the like through a thermochemical conversion process on the basis of the industrialization of the biomass pyrolysis gasification process which is mature day by day at present, so that the technology development direction is provided, and the problem of environmental pollution caused by the existing agricultural and forestry waste in China can be solved. Therefore, a new hydrogen production method is needed, which converts biomass into hydrogen energy, improves the utilization value of biomass, and solves the problem that the existing hydrogen production method depends on traditional energy sources.
Disclosure of Invention
The technical problem solved by the utility model is to provide a device for preparing hydrogen by biomass pyrolysis and gasification in a double fluidized bed, so as to solve the problems provided in the background technology.
The utility model provides a technical problem adopt following technical scheme to realize: an apparatus for preparing hydrogen by pyrolysis and gasification of biomass in a dual fluidized bed, comprising: the double fluidized bed comprises a fluidized bed pyrolysis furnace and a fluidized bed combustion furnace, wherein the fluidized bed pyrolysis furnace comprises a pyrolysis furnace riser, the rear end of the pyrolysis furnace riser is connected with a pyrolysis furnace cyclone separator, the upper part of the pyrolysis furnace cyclone separator is connected with a shift reactor, the lower part of the pyrolysis furnace cyclone separator is connected with a pyrolysis furnace material returning valve, the other outlet of the pyrolysis furnace material returning valve is connected with the fluidized bed combustion furnace, and the fluidized bed combustion furnace comprises a combustion furnace riser; the other outlet of the return valve of the pyrolysis furnace is connected with the bottom of the lifting pipe of the combustion furnace; an oxygen carrier cyclone separator is arranged in the middle of a combustion furnace lifting pipe, and CO is arranged at the top of the combustion furnace lifting pipe2An absorbent cyclone; the lower end of the oxygen carrier cyclone separator is connected to an oxygen carrier return valve, and the upper end of the oxygen carrier cyclone separator is connected with CO2The absorbent cyclone separator is connected; the other end of the oxygen carrier return valve is connected with the lower part of the pyrolysis furnace lifting pipe; CO 22The lower end of the absorbent cyclone is connected to CO2Absorbent return valve, CO2The other end of the absorbent return valve is connected with the lower part of a pyrolysis furnace lifting pipe; CO 22The outlet at the upper end of the absorbent cyclone 203 is connected to a separation cooling device.
Further, the separation cooling device is connected with a steam superheater in a navigation mode; the other side of the steam superheater is connected with the shift reactor; the steam superheater is also provided with an outlet which is connected with the upper part of the cyclone separator of the pyrolysis furnace and the booster fan; the other side of the booster fan is connected with the bottom of the pyrolysis furnace lifting pipe; the shift reactor is also provided with an interface to the gas separator.
Further, the carbon dioxide outlet of the gas separator is connected to a return valve of the pyrolysis furnace, an oxygen carrier return valve and CO2Absorbent return valve.
Furthermore, the middle part of the combustion furnace lifting pipe is provided with an expanding section and a secondary air distribution port.
Compared with the prior art, the beneficial effects of the utility model are that:
(1) the utility model does not need pure oxygen as gasifying agent in the preparation process, the system can meet the production requirement only by supplementing air as gasifying, the production cost is low, the pyrolysis furnace does not use air for fluidization, and the content of effective components in the biomass gas is high;
(2) the utility model improves the conversion rate of the biomass C element through the oxygen carrier, and improves the hydrogen production efficiency of the system;
(3) the utility model utilizes CO2Circulation of the absorbent in the furnace to remove CO from the pyrolysis furnace2Is carried into a combustion furnace to be released, and reduces CO in a pyrolysis furnace2Concentration to increase the forward reaction rate of the shift reaction;
(4) due to oxygen carrier and CO2The absorbent has larger density difference, and ensures the collection and return of bed materials with different densities by using height difference level collection on the basis of ensuring the efficiency of the combustion furnace and increasing the length of a combustion section.
(5) The utility model recovers the physical heat carried by the biomass ash, heats water, and further increases the superheat degree of steam by utilizing the sensible heat of the biomass gas, so that the biomass gas is close to the optimal working temperature of the shift reaction catalyst, and the reaction efficiency is improved;
(6) CO of the final product2The device is used by the return feeder of the return device, so that the slag bonding of the low-melting-point biomass at the return feeder is avoided.
(7) The utility model discloses directly change living beings into hydrogen energy utilization, the conversion rate is high, and the technology is advanced.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
In order to make the technical means, the creative features, the purpose and the efficacy of the present invention easily understood and appreciated, the present invention will be further explained with reference to the specific drawings, and in the description of the present invention, it should be noted that unless otherwise specified and limited, the terms "mounted", "connected" and "connected" should be understood broadly, for example, they may be fixed connection, detachable connection, or integrally connected, mechanically connected or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements.
As shown in fig. 1, an apparatus for preparing hydrogen by pyrolysis and gasification of dual fluidized bed biomass comprises: the double fluidized bed comprises a fluidized bed pyrolysis furnace 1 and a fluidized bed combustion furnace 2, wherein the fluidized bed pyrolysis furnace 1 comprises a pyrolysis furnace riser 101, the rear end of the pyrolysis furnace riser 101 is connected with a pyrolysis furnace cyclone 102, the upper part of the pyrolysis furnace cyclone 102 is connected with a shift reactor 103, the lower part of the pyrolysis furnace cyclone 102 is connected with a pyrolysis furnace material return valve 104, the other outlet of the pyrolysis furnace material return valve 104 is connected with the fluidized bed combustion furnace 2, and the fluidized bed combustion furnace 2 comprises a combustion furnace riser 201; the other outlet of the pyrolysis furnace material returning valve 104 is connected with the bottom of a combustion furnace lifting pipe 201; an oxygen carrier cyclone 202 is arranged in the middle of a combustion furnace lifting pipe 201, and CO is arranged at the top2An absorbent cyclone 203; the lower end of the oxygen carrier cyclone 202 is connected to an oxygen carrier return valve 205, and the upper end is connected with CO2The absorbent cyclone 203 is connected; the other end of the oxygen carrier return valve 205 is connected with the lower part of the pyrolysis furnace lifting pipe 101; CO 22The lower end of the absorbent cyclone 203 is connected to the CO2Absorbent return valve 206, CO2The other end of the absorbent return valve 206 is connected with the lower part of the pyrolysis furnace lifting pipe 101; CO 22The upper outlet of the absorbent cyclone 203 is connected to a separation cooling device 204.
The separation cooling device 204 is connected with a steam superheater 3 in a navigation way; the other side of the steam superheater 3 is connected to a shift reactor 103; the steam superheater 3 is also provided with an outlet which is connected with the upper part of the pyrolysis furnace cyclone separator 102 and the booster fan 4; the other side of the booster fan 4 is connected with the bottom of the pyrolysis furnace lifting pipe 101; the shift reactor 103 is also provided with an interface to the gas separator 5.
The 5-branch carbon dioxide outlet of the gas separator is connected with the return valve 104 of the pyrolysis furnace, the oxygen carrier return valve 205 and the CO2An absorbent return valve 205. Aims to prevent the biomass semi-coke or biomass ash with low ash fusion point from generating molten slagging without increasing the local temperature of a material returning valve.
The middle part of the combustion furnace lifting pipe 201 is provided with an expanding section and a secondary air distribution port 207. Aims at reducing the air velocity at the upper part of the fluidized bed, preventing the local high temperature at the bottom, improving the reaction temperature at the upper part, leading the combustion reaction to be more sufficient and carrying out CO reaction2The calcination of the absorbent is more sufficient, and the system efficiency is improved.
A method for preparing hydrogen by double fluidized bed biomass pyrolysis gasification comprises the following steps:
1) the biomass raw material is added into a pyrolysis furnace lifting pipe 101, and is subjected to pyrolysis and gasification reaction with a high-temperature oxygen carrier and hot combustion gas in the pyrolysis furnace lifting pipe to generate semicoke and pyrolysis gas. The pyrolysis gas is further mixed with CO added in the middle of the pyrolysis furnace lifting pipe 1012The absorbent reacts. Pyrolysis gas carries semicoke, oxygen carrier and CO2The absorbent is separated in a cyclone separator 102 of the pyrolysis furnace, and the semicoke, the oxygen carrier and the CO are separated2The absorbent enters a return valve 104 of the pyrolysis furnace, and the pyrolysis gas enters a connection shift reactor 103.
2) Semicoke, oxygen carrier, CO2The absorbent enters the bottom of the combustion furnace riser 201 to react with the introduced air after passing through the pyrolysis furnace return valve 104, and the oxygen carrier passes through the oxygen carrier cyclone 202 and is sent back to the bottom of the pyrolysis furnace riser 101 through the oxygen carrier return valve 205. CO 22Absorbent quilt CO2The absorbent cyclone 203 is fed with CO after collection2An absorbent return valve 206 and is returned to the bottom of the pyrolysis furnace riser 101And (4) a section.
3) Biomass ash fraction is CO2The absorbent cyclone 203 collects and partly enters the separating and cooling device 204, the cooled ash in the separating and cooling device 204 is discharged from the bottom, and the flue gas is discharged from the upper part of the separating and cooling device 204. Meanwhile, the steam generated by the separation cooling device 204 is sent to the steam superheater 3, and the generated superheated steam participates in the shift reaction in the shift reactor 103. The steam superheater 3 is heated by high-temperature fuel gas conveyed by the booster fan 4, and the high-temperature fuel gas passes through the booster fan 4 after being cooled and is finally conveyed to the bottom of the pyrolysis furnace lifting pipe 101.
4) The gas after the reaction in the shift reactor 103 is separated into hydrogen, carbon dioxide and natural gas by the gas separator 5. Wherein the carbon dioxide is delivered to the pyrolysis furnace return valve 104, the oxygen carrier return valve 205, the CO2An absorbent return valve 206 is used.
Specifically, the oxygen carrier performs a high temperature reaction at the bottom of the combustion furnace riser 201 to obtain oxygen atoms, and loses the oxygen atoms at the bottom of the pyrolysis furnace riser 101, and the oxygen atoms can be Ti-based, Mn-based or Cu-based oxygen carriers. Aims to carry oxygen atoms on the combustion side to the pyrolysis side, increase the amount of CO converted from biomass fixed carbon and further enhance CO + H2The amount of CO in the O reaction improves the reaction efficiency and the yield.
In particular, CO2The absorbent may be a lithium-based, calcium-based absorbent. Aims at reducing CO in the biomass gas2In an amount such that the shift reaction CO + H2O→CO2+H2The reaction is carried out in the positive reaction direction, and the conversion rate is improved.
Specifically, the steam superheating temperature is controlled to be close to 200-600 ℃ of the optimal working temperature of the catalyst for the shift reaction. Aims to homogenize the temperature field in the reactor, avoid the reduction of the working efficiency of the catalyst caused by uneven temperature and improve the reaction strength.
Example 1
Adding rice hulls into a pyrolysis furnace lifting pipe, reacting with ilmenite, calcium oxide and rice hull ash in the pyrolysis furnace lifting pipe, wherein the reaction temperature is 700 ℃, and generating semicoke and pyrolysis gas, wherein the pyrolysis gas mainly comprises the following components: 36% CO, 9% CO2，29％H2，13％CH4，4％CnHm，9％H2And O. Semicoke, oxygen carrier and CO are carried out through a cyclone separator of a pyrolysis furnace2Separating the absorbent and feeding the pyrolysis gas into a shift reactor.
Semicoke, oxygen carrier, CO2The absorbent enters the bottom of the riser of the combustion furnace to react with the introduced air at the temperature of 750 ℃, the oxygen carrier ilmenite is oxidized and collected by an oxygen carrier cyclone separator and sent back to the bottom of the riser of the pyrolysis furnace, and CO is2The absorbent (calcium oxide) is further heated to 850 ℃ at the middle upper part of the combustion furnace riser to be calcined and decomposed and is subjected to CO decomposition2And after being collected by the absorbent cyclone separator, the absorbent cyclone separator and part of the semicoke are returned to the bottom of a lifting pipe of the pyrolysis furnace.
And (3) after the reaction, the bed material with the grain size less than 350 microns enters a separation cooling device, is cooled to 80 ℃ and is discharged, meanwhile, the separation cooling device generates steam of 1.2Mpa, the bed material at 250 ℃ is conveyed to a steam superheater, and the steam superheater generates superheated steam at 450 ℃.
The superheated steam enters a shift reactor to complete the shift reaction. The shift reaction uses an iron-chromium catalyst, the reaction temperature is 435 ℃, and the fuel gas after the reaction is separated into 46% of hydrogen, 31% of carbon dioxide and 17% of natural gas through a gas separator. Wherein the carbon dioxide is delivered to a return valve of the pyrolysis furnace, an oxygen carrier return valve and CO2The temperature of the absorbent returning material valve is controlled at 600-700 ℃.
Example 2
The straw is added into a pyrolysis furnace lifting pipe to react with a copper-based oxygen carrier, a lithium-based absorbent and straw ash in the pyrolysis furnace lifting pipe, the reaction temperature is 550 ℃, semicoke and pyrolysis gas are generated, and the pyrolysis gas mainly comprises the following components: 32% CO, 14% CO2，24％H2，11％CH4，3％CnHm，16％H2And O. Semicoke, oxygen carrier and CO are carried out through a cyclone separator of a pyrolysis furnace2Separating the absorbent and feeding the pyrolysis gas into a shift reactor.
Semicoke, oxygen carrier, CO2The absorbent enters the bottom of a lifting pipe of the combustion furnace to react with the introduced air at the temperature of 640 ℃, a copper-based oxygen carrier is oxidized and passes through an oxygen carrier cyclone separatorCollecting and returning CO to the bottom of a riser of the pyrolysis furnace2The absorbent (lithium-based absorbent) is further heated to 680 ℃ at the upper part in the combustion furnace riser, is calcined and decomposed and is subjected to CO decomposition2And after being collected by the absorbent cyclone separator, the absorbent cyclone separator and part of the semicoke are returned to the bottom of a lifting pipe of the pyrolysis furnace.
After the reaction, the bed material with the grain size less than 200 microns enters a separation cooling device, is cooled to 60 ℃ and discharged, meanwhile, the separation cooling device generates steam of 0.5Mpa, the bed material with the grain size less than 200 microns is conveyed to a steam superheater, and the steam superheater generates superheated steam at 225 ℃.
The superheated steam enters a shift reactor to complete the shift reaction. The transformation reaction uses a copper-based low-temperature catalyst, the reaction temperature is 230 ℃, and the fuel gas after the reaction is separated into 42% of hydrogen, 34% of carbon dioxide and 15% of natural gas through a gas separator. Wherein the carbon dioxide is delivered to a return valve of the pyrolysis furnace, an oxygen carrier return valve and CO2The temperature of the absorbent returning material valve is controlled at 550-650 ℃.
Example 3
The wood chips are added into a pyrolysis furnace lifting pipe to react with a manganese-based oxygen carrier, calcium oxide and wood ash in the pyrolysis furnace lifting pipe, the reaction temperature is 800 ℃, semicoke and pyrolysis gas are generated, and the pyrolysis gas mainly comprises the following components: 41% CO, 8% CO2，32％H2，12％CH4，2％CnHm，5％H2And O. Semicoke, oxygen carrier and CO are carried out through a cyclone separator of a pyrolysis furnace2Separating the absorbent and feeding the pyrolysis gas into a shift reactor.
Semicoke, oxygen carrier, CO2The absorbent enters the bottom of a combustion furnace riser and reacts with the introduced air at the temperature of 880 ℃, the manganese-based oxygen carrier is oxidized and collected by an oxygen carrier cyclone separator and sent back to the bottom of the pyrolysis furnace riser, and CO is2The absorbent (calcium oxide) is further heated to 950 ℃ in the middle upper part of the combustion furnace riser to be calcined and decomposed and is subjected to CO decomposition2And after being collected by the absorbent cyclone separator, the absorbent cyclone separator and part of the semicoke are returned to the bottom of a lifting pipe of the pyrolysis furnace.
And (3) after the reaction, the bed material with the grain size less than 100 microns enters a separation cooling device, is cooled to 60 ℃ and is discharged, meanwhile, the separation cooling device generates steam of 1.6Mpa, the bed material at 300 ℃ is conveyed to a steam superheater, and the steam superheater generates superheated steam at 485 ℃.
The superheated steam enters a shift reactor to complete the shift reaction. The transformation reaction uses cobalt metal catalyst, the reaction temperature is 600 ℃, and the fuel gas after the reaction is divided into 49% of hydrogen, 32% of carbon dioxide and 12% of natural gas through a gas separator. Wherein the carbon dioxide is delivered to a return valve of the pyrolysis furnace, an oxygen carrier return valve and CO2The temperature of the absorbent returning material valve is controlled to be 800-900 ℃.
The utility model discloses a double fluidized bed device accomplishes the pyrolysis and gasification reaction of living beings in the pyrolysis side, produces living beings gas and living beings semicoke. Biomass and high-temperature circulating ash, oxygen carrier and CO2The absorbent is subjected to pyrolysis reaction, the reacted biomass semicoke further reacts with oxygen atoms in the oxygen carrier to generate carbon monoxide, and simultaneously the carbon dioxide and the CO generated by the reaction2The absorbent reacts to form carbonates. The biomass gas is subjected to a shift reaction with water vapor, and mainly the carbon monoxide carried by the biomass gas reacts with the water vapor to generate hydrogen and carbon dioxide; wherein the concentration of carbon dioxide in the fuel gas is reduced, thereby facilitating the forward progress of the reaction.
The basic principles and the main features of the invention and the advantages of the invention have been shown and described above. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.

Claims (4)

1. An apparatus for preparing hydrogen by pyrolysis and gasification of biomass in a dual fluidized bed, comprising: the double fluidized bed comprises a fluidized bed pyrolysis furnace and a fluidized bed combustion furnace, and is characterized in that: the fluidized bed pyrolysis furnace comprises a pyrolysis furnace lifting pipe, the rear end of the pyrolysis furnace lifting pipe is connected with a pyrolysis furnace cyclone separator, and the pyrolysis furnace cyclone separator is arranged on the rear end of the pyrolysis furnace lifting pipeThe upper part of the furnace cyclone separator is connected with the shift reactor, the lower part of the furnace cyclone separator is connected with a return valve of the pyrolysis furnace, the other outlet of the return valve of the pyrolysis furnace is connected with a fluidized bed combustion furnace, and the fluidized bed combustion furnace comprises a combustion furnace riser; the other outlet of the return valve of the pyrolysis furnace is connected with the bottom of the lifting pipe of the combustion furnace; an oxygen carrier cyclone separator is arranged in the middle of a combustion furnace lifting pipe, and CO is arranged at the top of the combustion furnace lifting pipe2An absorbent cyclone; the lower end of the oxygen carrier cyclone separator is connected to an oxygen carrier return valve, and the upper end of the oxygen carrier cyclone separator is connected with CO2The absorbent cyclone separator is connected; the other end of the oxygen carrier return valve is connected with the lower part of the pyrolysis furnace lifting pipe; CO 22The lower end of the absorbent cyclone is connected to CO2Absorbent return valve, CO2The other end of the absorbent return valve is connected with the lower part of a pyrolysis furnace lifting pipe; CO 22An outlet at the upper end of the absorbent cyclone is connected to a separation cooling device.
2. The device for preparing hydrogen by pyrolysis and gasification of double fluidized beds of biomass according to claim 1, wherein: the separation cooling device is connected with a steam superheater in a navigation way; the other side of the steam superheater is connected with the shift reactor; the steam superheater is also provided with an outlet which is connected with the upper part of the cyclone separator of the pyrolysis furnace and the booster fan; the other side of the booster fan is connected with the bottom of the pyrolysis furnace lifting pipe; the shift reactor is also provided with an interface to the gas separator.
3. The device for preparing hydrogen by pyrolysis and gasification of double fluidized beds of biomass according to claim 2, wherein: the carbon dioxide outlet of the gas separator is connected with the return valve of the pyrolysis furnace, the oxygen carrier return valve and the CO2Absorbent return valve.
4. The device for preparing hydrogen by pyrolysis and gasification of double fluidized beds of biomass according to claim 1, wherein: the middle part of the combustion furnace lifting pipe is provided with an expanding section and a secondary air distribution port.
CN201920233990.1U 2019-02-25 2019-02-25 Device for preparing hydrogen by double fluidized bed biomass pyrolysis gasification Active CN209872347U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109704278A (en) * 2019-02-25 2019-05-03 合肥德博生物能源科技有限公司 A kind of device and method that double-fluidized-bed biomass pyrogenation gasification prepares hydrogen
CN114044490A (en) * 2022-01-13 2022-02-15 浙江百能科技有限公司 Device and method for preparing hydrogen-rich gas based on double fluidized bed pyrolysis gas conversion

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109704278A (en) * 2019-02-25 2019-05-03 合肥德博生物能源科技有限公司 A kind of device and method that double-fluidized-bed biomass pyrogenation gasification prepares hydrogen
CN114044490A (en) * 2022-01-13 2022-02-15 浙江百能科技有限公司 Device and method for preparing hydrogen-rich gas based on double fluidized bed pyrolysis gas conversion
CN114044490B (en) * 2022-01-13 2022-05-13 浙江百能科技有限公司 Device and method for preparing hydrogen-rich gas based on double fluidized bed pyrolysis gas conversion

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