CN101870455B - Chain type hydrogen and oxygen production integrated method and device - Google Patents

Chain type hydrogen and oxygen production integrated method and device Download PDF

Info

Publication number
CN101870455B
CN101870455B CN2010102198926A CN201010219892A CN101870455B CN 101870455 B CN101870455 B CN 101870455B CN 2010102198926 A CN2010102198926 A CN 2010102198926A CN 201010219892 A CN201010219892 A CN 201010219892A CN 101870455 B CN101870455 B CN 101870455B
Authority
CN
China
Prior art keywords
cufe
seal valve
reaction
reactor
zro
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
CN2010102198926A
Other languages
Chinese (zh)
Other versions
CN101870455A (en
Inventor
王保文
赵海波
郑瑛
张少华
郑楚光
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Huazhong University of Science and Technology
Original Assignee
Huazhong University of Science and Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Huazhong University of Science and Technology filed Critical Huazhong University of Science and Technology
Priority to CN2010102198926A priority Critical patent/CN101870455B/en
Publication of CN101870455A publication Critical patent/CN101870455A/en
Application granted granted Critical
Publication of CN101870455B publication Critical patent/CN101870455B/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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

Abstract

The invention provides a chain type hydrogen and oxygen production integrated method, comprising the following steps: CuFe2O4 and solid carbonaceous matters are subjected to reduction reaction to obtain reduction products of Cu, Fe and FeO, wherein the Fe, the FeO and vapour are subjected to oxidation reaction to generate H2 and Fe3O4, and the residual Cu is in oxidation reaction with the Fe3O4 and air to generate CuFe2O4 by oxidation; and the CuFe2O4 is heated and decomposed to generate O2 and CuFeO2, and the CuFeO2 and air are in oxidation reaction to generate CuFe2O4 once again. The invention also provides a device for realizing the method, which comprises the main assemblies of a bubbling fluidized bed reactor, a cyclone separator, a sealing valve and a rapid fluidized bed. The invention can obtain H2 and O2 by chain type continuous preparation, has simple process and low energy consumption, can obtain H2 and O2 with the high purity approximate to 100%, realizes CO2 zero emission in the hydrogen production process and has broad application prospect.

Description

Chain type hydrogen and oxygen production integrated method and device
Technical field
The present invention relates to hydrogen H 2And O 2Preparation field is specifically related to the high-purity H of continuous preparation of a kind of while 2And O 2Method and apparatus.
Background technology
H 2Be not only a kind of important chemical material, still a kind of energy carrier of high effect cleaning all has a wide range of applications at aspects such as oil, chemical industry, traffic, electric power.Current, the preparation of hydrogen has received close concern, and the preparation method of hydrogen is very many, but employed most of H is gone up in industry 2Still come from the electrolysis of water, perhaps with hydrocarbon gas fuel be raw material, and through hydrocarbon gas fuel reforming, steam transform, CO 2Remove and H 2Many processes such as separation purification and obtain, but because brine electrolysis system H 2Energy consumption is high, and hydrocarbon gas fuel reforming system H 2The time system complex, efficient is low, cost is high, is difficult to obtain high-purity H 2Thereby, make the mass preparation and the H of above-mentioned technology 2Widespread use received great restriction.
Simultaneously, O 2Be not only the important substance that the human life is able to maintain, and all have a wide range of applications at medical treatment, health care and other commercial run, so O 2Preparation also be a very crucial technology.Mainly be to obtain at present through low temperature fractionation or pressure-swing adsorption process.Low temperature fractionation is mainly according to N in the air 2And O 2The difference of boiling point, air is compressed and liquefied, carry out low temperature fractionation and make O 2From air, separate, although with a long history, the technology maturation of this method, investment is big, energy consumption is high, the construction period is long, complicated operation; Pressure swing adsorption process then mainly based on sorbent materials such as molecular sieves to N in the air 2And O 2Selective adsorption performance difference and from air, obtain O 2, but owing to high energy consumption, low O 2Defectives such as purity make this method be difficult to widespread use.
Summary of the invention
The object of the present invention is to provide a kind of chain type hydrogen and oxygen production integrated method, can prepare high purity H simultaneously continuously near 100% 2And O 2, have less energy consumption, low, the CO of cost 2The advantage of zero release.
Another object of the present invention is to provide the device of realizing aforesaid method, can prepare high purity H simultaneously continuously near 100% 2And O 2, system is simple, be convenient to operation.
Chain type hydrogen and oxygen production integrated method is specially:
(1) with CuFe 2O 4Make reduction reaction with solid carbonaceous substance, obtain Cu, Fe, FeO;
(2) Fe, FeO and the water vapour that step (1) are obtained carry out oxidizing reaction, generate to give birth to hydrogen and Fe 3O 4
(3) Fe that Cu that step (1) is obtained and step (2) obtain 3O 4Carry out oxidizing reaction with air, regeneration forms CuFe 2O 4
(4) CuFe that step (3) is generated 2O 4Thermal degradation obtains O 2And CuFeO 2
(5) with CuFeO 2Carry out oxidizing reaction with air, regeneration forms CuFe 2O 4
CuFe in the said step (1) 2O 4With ZrO 2Mix the back and participate in reduction reaction.
Said step (3) is being doped with ZrO 2Condition under carry out oxidizing reaction.
Realize the device of aforesaid method; Bubbling bed reduction reactor 1, first seal valve 4, bubbling bed hydrogen-manufacturing reactor 5, first cyclonic separator 6, second seal valve 7, bubbling bed one-level oxygen making reaction device 8, second cyclonic separator 9, the 3rd seal valve 10, the bubbling bed two-stage system oxygen reactor 11, the 3rd cyclonic separator 12, the 4th seal valve 13 and the fast fluidized bed air reactor 14 that comprise pipe connection successively; Fast fluidized bed air reactor 14 also is connected with bubbling bed reduction reactor 1 with the 5th seal valve 16 through the 4th cyclonic separator 15, and bubbling bed reduction reactor 1 is connected to the 5th cyclonic separator 2 and the 6th seal valve 3 successively.
Technique effect of the present invention is embodied in:
1, be raw material with coal or other carbonaceousfuel (comprising biomass, mud), reserves are big, the source is wide, price is low.
2, with CuFe 2O 4/ ZrO 2As oxygen carrier, the doping of Cu component has improved the rate of reduction of Fe oxide compound effectively, and ZrO 2As inert support, improved the anti-agglutinatting property ability of this oxygen carrier, improved the mechanical property of this oxygen carrier; Guarantee that this oxygen carrier reactivity worth in hydrogen manufacturing repeatedly and system oxygen cycle process can not decay; Do not wear and tear, not broken, structure properties is able to effectively keep, general above-mentioned ZrO 2Account for CuFe 2O 4With ZrO 2Mixed mass percent is smaller or equal to 10%.
3, with CuFe 2O 4/ ZrO 2As oxygen carrier, be used for chain type hydrogen and oxygen production integrated process, its response characteristic is fully utilized.Theoretical foundation is following:
The molecular formula of supposing carbonaceousfuels such as coal is reduced to C, in reduction reactor, and carbonaceousfuel and CuFe such as coal 2O 4/ ZrO 2The complicated reaction of series takes place in oxygen carrier, and is specific as follows:
At first, under steam atmosphere, carbonaceousfuels such as coal absorb certain heat generating gasification reaction, produce CO and H 2Gas, concrete shown in (1) formula.
C+H 2O (gas) → H 2(gas)+CO (gas)
(1)
And remaining coal tar particle comes back in the reduction reactor through outer loop, in rich H 2O steam and CO 2Under the atmosphere, transform (seeing formula (2)) and gasification reaction (seeing formula (3)), specific as follows:
Coke C+H 2O (gas) → H 2(gas)+CO (gas)
(2)
Coke C+CO 2(gas) → 2CO (gas)
(3)
Gasification product H 2, CO and CuFe 2O 4/ ZrO 2Oxygen carrier generation oxidizing reaction generates water vapour, Cu, FeO (perhaps Fe) and ZrO respectively 2And CO 2Gas also discharges heat, reacts specific as follows:
H 2(gas)+0.5CuFe 2O 4/ ZrO 2→ 0.5Cu+FeO+0.5ZrO 2+ H 2O (gas) (4)
H 2(gas)+0.25CuFe 2O 4/ ZrO 2→ 0.25Cu+0.5Fe+0.25ZrO 2+ H 2O (gas) (5)
CO (gas)+0.5CuFe 2O 4/ ZrO 2→ 0.5Cu+FeO+0.5ZrO 2+ CO 2(gas)
(6)
CO (gas)+0.25CuFe 2O 4/ ZrO 2→ 0.25Cu+0.5Fe+0.25ZrO 2+ CO 2(gas) (7)
Secondly, in the hydrogen reaction device, be reduced the FeO or Fe and the vapor generation that obtain
Steam iron reaction (seeing formula (8)) generates H 2, and discharge little heat, and resultant after the residual water vapor condensation be exactly purity near 100% H 2, react specific as follows:
3Fe+ (Cu+ZrO 2)+4H 2O (gas) → Fe 3O 4+ (Cu+ZrO 2)+4H 2(gas)
(8)
3FeO+ (Cu+ZrO 2)+H 2O (gas) → Fe 3O 4+ (Cu+ZrO 2)+4H 2(gas)
(9)
Then, in the two-stage oxygen generation system, by the Fe of water vapour partially oxidation generation 3O 4With Cu, ZrO 2In one-level oxygen making reaction device with air (3.76N just 2+ O 2) oxidizing reaction takes place, discharge a large amount of heats, and oxidation generates CuFe 2O 4/ ZrO 2Oxygen carrier (like reaction (10)), this oxygen carrier thermal endothermic decomposition in the two-stage system oxygen reactor discharges O 2, the water vapour as fluidization medium carried out condensation after, just can obtain purity near high-purity O of 100% 2The concrete reaction as follows:
2Fe 3O 4+3Cu+3ZrO 2+2(3.76N 2+O 2)→3CuFe 2O 4/ZrO 2+7.52N 2
(10)
CuFe 2O 4/ ZrO 2→ CuFeO 2+ O 2(gas)+ZrO 2
(11)
At last, decomposition obtains CuFeO 2With ZrO 2Again in air reactor with air (3.76N just 2+ O 2) carry out oxidizing reaction, form CuFe again 2O 4/ ZrO 2Oxygen carrier, concrete reaction formula be suc as formula shown in (12), and emit a large amount of heats:
CuFeO 2+ZrO 2+(3.76N 2+O 2)→CuFe 2O 4/ZrO 2+3.76N 2
(12)
Through above-mentioned analysis, can find out CuFe 2O 4In whole process of preparation,, constantly be repeated to utilize, produce H continuously through twice regeneration 2And O 2
4, this process prepares is concentration near 100% high purity H 2And O 2, do not contain other to human body and the deleterious impurity of environment;
5, because solid carbon fuel reserves such as coal are big, low price, distribution are extensive, avoided traditional industry system H simultaneously 2The time many complex processes (comprise that hydrocarbon gas fuel reforming, steam transform, CO 2Remove and H 2Separation purification etc.), make hydrogen manufacturing cost and energy consumption thereof be effectively controlled; While CuFe 2O 4/ ZrO 2The temperature that oxygen carrier decomposes release of oxygen is lower, is no more than 1000 ℃, and required caloric receptivity can provide through the waste heat of other thermopositive reaction in the system fully, therefore makes O 2The time energy consumption also can effectively reduce.
6, last, because CuFe 2O 4/ ZrO 2Oxygen carrier is in different reactor drums, to carry out with the reduction reaction of carbonaceousfuels such as coal and the oxidizing reaction of reduction product Fe and FeO and water vapour, has realized hydrogen production process CO 2Zero release.
Description of drawings
Fig. 1 is apparatus of the present invention structure iron.
Fig. 2 is the inventive method schematic flow sheet.
Embodiment
Chain type hydrogen and oxygen production integrated device proposed by the invention, shown in Figure 1 like structure, form the oxygen carrier reduction reactor A of system by the cyclonic separator 2 of bubbling bed reduction reactor 1, separated oxygen carrier fine powder and coke particle thereof and seal valve 3 and seal valve 4; Form hydrogen generating system B by bubbling bed hydrogen-manufacturing reactor 5, cyclonic separator 6 and seal valve 7 again; And then form oxygen generation system C by bubbling bed one-level oxygen making reaction device 8, cyclonic separator 9, seal valve 10, bubbling bed two-stage system oxygen reactor 11, cyclonic separator 12 and seal valve 13; At last, form the oxygen carrier regeneration system rapidly by fast fluidized bed air reactor 14, cyclonic separator 15 and seal valve 16 again.
In view of carbonic solid fuels such as coal gasification last residual Jiao in back and CuFe 2O 4/ ZrO 2For the oxygen carrier speed of reaction slow; Make carbonic solid fuels such as coal be difficult to abundant conversion, therefore, on the basis of reduction reactor 1 body; Used the external placed type recovery system that comprises cyclonic separator 2 and seal valve 3, made and fail the tiny coke and the CuFe of fully reaction 2O 4/ ZrO 2The oxygen carrier particle can reclaim again and get into the reduction reactor bottom, has not only improved the residence time of coke particle in reduction reactor effectively, and at reduction reactor bottom, the water vapour of high density and CO 2Atmosphere has promoted the abundant gasification and the conversion of coke particle, has guaranteed the abundant oxidation and the CuFe of carbonic solid fuels 2O 4/ ZrO 2The abundant reduction of oxygen carrier.
The present invention is with solid carbonaceous substance (comprising coal, biomass, mud etc.) and CuFe 2O 4/ ZrO 2Be raw material, carry out a series of reaction process, generate high-purity H 2And O 2, specifically shown in schematic flow sheet 2, specifically set forth as follows:
1. at first get in the reduction reactor 1, under the effect of temperature of reaction about 900 ℃ and water vapour fluidization medium, complex series of reactions (concrete shown in reaction formula (1)-(7)) takes place, a large amount of water vapour and CO that the carbonaceousfuel reaction generates 2And some the tiny coke and the CuFe that carry 2O 4/ ZrO 2Particle then separates through cyclonic separator 2, CO 2With water vapour resulting high concentration CO after condensation process 2Carry out aftertreatments such as geology storage, and coke that is recovered to and CuFe 2O 4/ ZrO 2Particle is then introduced the reduction reactor bottom through seal valve 3, at the CO of high density 2With steam atmosphere further reaction down;
2. be reduced Cu, Fe, FeO and the ZrO of generation 2Then get in the bubbling bed hydrogen reaction device 5 Deng the solid phase reduction product, carry out oxidizing reaction, produce hydrogen and small portion of residual water vapour, can make high-purity H after the condensation with water vapour through seal valve 4 2
3. the Fe that then, is formed by the water vapour partially oxidation 3O 4With Cu, ZrO 2Be transported in the one-level oxygen reaction device 8 through cyclonic separator 6 and seal valve 7 Deng together, fully react with air, oxidation generates CuFe 2O 4/ ZrO 2The oxygen carrier particle;
4. the CuFe of oxidation generation then, 2O 4/ ZrO 2The oxygen carrier particle gets in the secondary oxygen reaction device 11 through cyclonic separator 9 and seal valve 10 respectively again, decomposes the O that generates a certain amount of water vapour fluidization medium that mixes 2In, just can obtain purity near high-purity O of 100% through follow-up condensation process 2
5. last, decompose the CuFeO that generates 2With ZrO 2Get in the air reactor 14 through cyclonic separator 12 and seal valve 12 more together, carry out oxidizing reaction with air, regeneration forms complete CuFe 2O 4/ ZrO 2The oxygen carrier particle.
As regenerated CuFe 2O 4/ ZrO 2When the oxygen carrier particle delivered into reduction reactor 1 upper end through cyclonic separator 15 and seal valve 16 more again, said process constantly repeatedly repeated, thereby just continuously continuous chain type prepares high-purity H 2And O 2

Claims (4)

1. chain type hydrogen and oxygen production integrated method is specially:
(1) with CuFe 2O 4Make reduction reaction with solid carbon fuel, obtain Cu, Fe, FeO;
(2) Fe, FeO and the water vapour that step (1) are obtained carry out oxidizing reaction, generate to give birth to hydrogen and Fe 3O 4
(3) Fe that Cu that step (1) is obtained and step (2) obtain 3O 4Carry out oxidizing reaction with air, regeneration forms CuFe 2O 4
(4) CuFe that step (3) is generated 2O 4Thermal degradation obtains O 2And CuFeO 2
(5) with CuFeO 2Carry out oxidizing reaction with air, regeneration forms CuFe 2O 4
2. chain type hydrogen and oxygen production integrated method according to claim 1 is characterized in that, the CuFe in the said step (1) 2O 4With ZrO 2Mix the back and participate in reduction reaction.
3. chain type hydrogen and oxygen production integrated method according to claim 2 is characterized in that, said step (3) is being doped with ZrO 2Condition under carry out oxidizing reaction.
4. realize the device of the said method of claim 1, comprise bubbling bed reduction reactor (1), first seal valve (4), bubbling bed hydrogen-manufacturing reactor (5), first cyclonic separator (6), second seal valve (7), bubbling bed one-level oxygen making reaction device (8), second cyclonic separator (9), the 3rd seal valve (10), bubbling bed two-stage system oxygen reactor (11), the 3rd cyclonic separator (12), the 4th seal valve (13) and the fast fluidized bed air reactor (14) of pipe connection successively; Fast fluidized bed air reactor (14) also is connected with bubbling bed reduction reactor (1) with the 5th seal valve (16) through the 4th cyclonic separator (15); Bubbling bed reduction reactor (1) connects the 5th cyclonic separator (2) and the 6th seal valve (3) in addition respectively, and the 5th cyclonic separator (2) joins with the 6th seal valve (3).
CN2010102198926A 2010-07-08 2010-07-08 Chain type hydrogen and oxygen production integrated method and device Expired - Fee Related CN101870455B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2010102198926A CN101870455B (en) 2010-07-08 2010-07-08 Chain type hydrogen and oxygen production integrated method and device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2010102198926A CN101870455B (en) 2010-07-08 2010-07-08 Chain type hydrogen and oxygen production integrated method and device

Publications (2)

Publication Number Publication Date
CN101870455A CN101870455A (en) 2010-10-27
CN101870455B true CN101870455B (en) 2012-05-09

Family

ID=42995572

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2010102198926A Expired - Fee Related CN101870455B (en) 2010-07-08 2010-07-08 Chain type hydrogen and oxygen production integrated method and device

Country Status (1)

Country Link
CN (1) CN101870455B (en)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103062787B (en) * 2012-12-15 2015-07-22 华中科技大学 Method and device for burning pulverized coal with self-heating oxygen generation function
CN103274361B (en) * 2013-05-28 2015-02-25 东北大学 Oxygen-hydrogen co-production device and method based on chemical chain reaction
CN106244241B (en) * 2016-07-19 2018-12-14 东南大学 A kind of coal gasification preparing synthetic gas and chemical chain oxygen-hydrogen manufacturing combined cycle power plant and method
CN106629607B (en) * 2016-11-18 2019-01-15 武汉理工大学 A kind of pressure oxidation chemical chain making oxygen by air separation device and method for producing oxygen through
JP7085530B2 (en) * 2017-03-27 2022-06-16 住友重機械工業株式会社 Hydrogen production equipment and hydrogen production method
CN109019510A (en) * 2018-09-25 2018-12-18 上海涛川能源科技有限公司 A kind of hydrogen production process
CN111422830A (en) * 2020-05-18 2020-07-17 中国华能集团清洁能源技术研究院有限公司 Sewage treatment plant biogas hydrogen production system and method
CN112079333B (en) * 2020-09-07 2022-08-09 东方电气集团东方锅炉股份有限公司 Chain reaction hydrogen production system and hydrogen production method

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1791462A (en) * 2003-05-20 2006-06-21 出光兴产株式会社 Reforming catalyst for oxygen-containing hydrocarbon, method for producing hydrogen or synthesis gas using same, and fuel cell system
WO2008036902A2 (en) * 2006-09-21 2008-03-27 Eltron Research & Development, Inc. Cyclic catalytic upgrading of chemical species using metal oxide materials

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1791462A (en) * 2003-05-20 2006-06-21 出光兴产株式会社 Reforming catalyst for oxygen-containing hydrocarbon, method for producing hydrogen or synthesis gas using same, and fuel cell system
WO2008036902A2 (en) * 2006-09-21 2008-03-27 Eltron Research & Development, Inc. Cyclic catalytic upgrading of chemical species using metal oxide materials

Non-Patent Citations (5)

* Cited by examiner, † Cited by third party
Title
Fuels》.2006,第20卷1836-1844. *
Kyoung-Soo Kang et al..Redox cycling of CuFe2O4 supported on ZrO2 and CeO2 for two-step methane reforming/water splitting.《International journal of hydrogen energy》.2009,第35卷568-576. *
Yan Cao et al..Investigation of Chemical Looping Combustion by Solid Fuels. 1.Process Analysis.《Energy & Fuels》.2006,第20卷1836-1844.
Yan Cao et al..Investigation of Chemical Looping Combustion by Solid Fuels. 1.Process Analysis.《Energy &amp *
郝建刚等.基于Fe 基载氧体的生物质化学链燃烧试验研究.《锅炉技术》.2010,第41卷(第2期),65-70. *

Also Published As

Publication number Publication date
CN101870455A (en) 2010-10-27

Similar Documents

Publication Publication Date Title
CN101870455B (en) Chain type hydrogen and oxygen production integrated method and device
US9617478B2 (en) Process and apparatus for converting greenhouse gases into synthetic fuels
CN102408095B (en) Method of decomposing hydrogen sulfide for preparation of hydrogen and elemental sulfur
US7829051B2 (en) Production and uses of carbon suboxides
CN101671002B (en) Method and device for preparing hydrogen by using fuel
CN103062910B (en) Method and device for integrating chemical-looping combustion with CO<2> trapping
CN106629600B (en) Crude synthesis gas adsoption catalysis process for making hydrogen and its equipment
CN101962575B (en) Method and device for preparing synthesis gas by coal particle/oxygen carrier chemical chain
CN101672530A (en) Method and device for burning chemistry chains based on iron or iron oxide
CN102219183B (en) Double-circulation chained combustion hydrogen heat coproduction and CO2 separating method and device thereof
CN101439844A (en) Chemical link coupling catalytic reforming hydrogen making method and device
US20200317526A1 (en) Processes for converting carbon dioxide
CN104591083A (en) Hydrogen preparation method
CN110951508A (en) Device and process for preparing methane by coal chemical-looping catalytic gasification based on calcium oxide
CN101746721A (en) Method and device for producing hydrogen and separating CO2 based on iron or iron oxide
CN113353920B (en) Continuous preparation device and preparation method of carbon nano tube
CN101607859B (en) Process employing coke-oven gas for production of methane
CN113072981B (en) Chemical chain deoxidation gasification synergistic CO for functional composite oxygen carrier2Transformation method
WO2021232663A1 (en) System and method for producing hydrogen from biogas in sewage treatment plant
CN101284763B (en) Process for preparing ethandiol for end gas of calcium carbide furnace
CN1195171C (en) Coal fired serial fluidized bed indirect burning device and method
CN101830434A (en) Method for producing synthetic gas by natural gas conversion
CN201770472U (en) Solid fuel fluidized bed near-zero emission hydrogen production device
CN101995097A (en) Fuel reactor device for chemical-looping combustion
CN112158805B (en) Method and system for preparing hydrogen by using biomass

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
CF01 Termination of patent right due to non-payment of annual fee
CF01 Termination of patent right due to non-payment of annual fee

Granted publication date: 20120509

Termination date: 20180708