CN102219183A - Double-circulation chained combustion hydrogen heat coproduction and CO2 separating method and device thereof - Google Patents
Double-circulation chained combustion hydrogen heat coproduction and CO2 separating method and device thereof Download PDFInfo
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- CN102219183A CN102219183A CN2011101067611A CN201110106761A CN102219183A CN 102219183 A CN102219183 A CN 102219183A CN 2011101067611 A CN2011101067611 A CN 2011101067611A CN 201110106761 A CN201110106761 A CN 201110106761A CN 102219183 A CN102219183 A CN 102219183A
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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
Abstract
The invention discloses a double-circulation chained combustion hydrogen heat coproduction and CO2 separating method and a device thereof. Fe2O3 is reduced by fuel gas in a fuel reactor fluidized bed of a hydrogen production system to obtain solid product FeO or Fe; the FeO or Fe enters into a water vapour reactor fluidized bed of the hydrogen production system to be reacted with water vapour so as to generate hydrogen and Fe3O4, gas at an outlet is condensed, and water is separated to obtain pure H2; the Fe3O4 enters into an air reactor fluidized bed of the hydrogen production system to be calcined so as to regenerate Fe2O3, and the Fe2O3 is recycled; smoke discharged from the fuel reactor fluidized bed of the hydrogen production system is introduced into a fuel fluidized bed of a heating system, residual fuel gas in the smoke reacts with NiO to obtain gas products such as the water vapour and CO2, and pure CO2 is obtained after the water contained in the gas products is condensed and separated; and the solid product Ni enters into the air reactor fluidized bed of the heating system to be calcined with air, heat is released, the solid product NiO is obtained, and the NiO is regenerated and the next circulation is carried out.
Description
Technical field
The present invention relates to utilize carbonaceous fuel gas to produce the method and apparatus of hydrogen, relate in particular to a kind of carbonaceous fuel gas that utilizes and produce hydrogen and capture CO through chain type circulation
2Method and apparatus.
Background technology
Hydrogen, as a kind of energy, directly combustion power generation, heat supply or be used for portable power source by fuel cell.Hydrogen is in the conversion process of energy, and following product is water.Hydrogen can really be realized the zero release of pollutent as a kind of free of contamination secondary energy.Along with global warming and environmental pollution increasingly sharpen, hydrogen is expected to become the important energy carrier in the near future.Hydrogen mainly is used as industrial chemicals but not the energy at present, and it produces main reformation or gasification by fossil oil.Fossil oil can produce carbonic acid gas in producing the process of hydrogen.Carbonic acid gas is a kind of typical greenhouse gases, if with hydrogen as fuel and in the process of hydrogen manufacturing, carbonic acid gas is not captured and is discharged in the atmosphere, with the Global climate change of directly aggravating Greenhouse effect and being caused.Hydrogen will disappear as the advantage of eco-friendly secondary energy.It is the country of main fuel with the coal that China is one, under this fundamental realities of the country, the selection of hydrogen source mainly comes from the fossil oil based on coal, thus utilize cleanly and efficiently based on the fossil oil of coal produce hydrogen and effectively capturing carbon dioxide become one of key of fossil oil cleaning hydrogen manufacturing.
Summary of the invention
The invention provides hot coproduction of a kind of pair of circulation chain type hydrogen combusted and separation of C O
2Method and device thereof.The present invention effective separation of C O when utilizing carbonaceous fuel gas to produce hydrogen
2, and produce additional heat, have the greenhouse gas emission of minimizing and the high advantage of energy conversion efficiency.
Method and technology scheme of the present invention is as follows:
Hot coproduction of a kind of pair of circulation chain type hydrogen combusted and separation of C O
2Method, iron is placed the air reactor fluidized-bed of hydrogen generating system, at the air reactor fluidized-bed lower end of hydrogen generating system bubbling air, the air reactor bottom compartment of hydrogen generating system is in bubbling fluidization; The temperature of the air reactor fluidized-bed of hydrogen generating system is controlled at 1000 ℃; Iron and airborne oxygen reaction generate Fe
2O
3Fe
2O
3Through the air reactor transition section of hydrogen generating system and the air reactor riser tube of hydrogen generating system, by the air cyclonic separator of air-lift unit to hydrogen generating system, through gas solid separation, Fe
2O
3Air reactor tremie pipe by hydrogen generating system enters in the fuel reaction device of hydrogen generating system; The temperature of the fuel reaction device of hydrogen generating system is controlled at 900 ℃; The fuel reaction device fluidized-bed lower end of hydrogen generating system feeds carbonaceous fuel gas, and the fuel reaction device of hydrogen generating system is in bubbling fluidization, Fe
2O
3Be reduced to FeO or Fe; FeO or Fe enter the water vapour reactor fluidisation bed of hydrogen generating system through overflow groove; Water vapour reactor fluidisation bed lower end at hydrogen generating system feeds water vapour, and water vapour reactor bottom compartment is in bubbling fluidization, and the temperature of the water vapour reactor fluidisation bed of hydrogen generating system is controlled at 650 ℃; The also FeO of ortho states or Fe and water vapour reaction, solid product is Fe
3O
4, gaseous product is H
2Fe
3O
4Process water vapour reactor transition section and water vapour reactor riser are to the hydrogen cyclonic separator, and gas-solid is through separating solid product Fe
3O
4Enter the air reactor fluidized-bed of hydrogen generating system through water vapour reactor tremie pipe and water vapour reactor overflow groove, gaseous product then through the hydrogen cyclonic separator outlet overflow, condensation separation obtains purified H after going out wherein water
2Enter the Fe of the air reactor fluidized-bed of hydrogen generating system
3O
4With air calcination, Fe
3O
4Be converted into Fe
2O
3, Fe
2O
3Realize recycle; The flue gas that comes out from the fuel reaction device of hydrogen generating system enters the fuel reaction device bottom air compartment the fuel reaction device fluidized-bed of heating by pipe connecting; Add NiO in the fuel reaction device fluidized-bed of heating, the fuel reaction device in the fuel reaction device fluidized-bed is in bubbling fluidization; The temperature of the fuel reaction device of heating is controlled at 900 ℃; NiO with from the residual fuel gas reaction in the fuel reaction device flue gas of hydrogen generating system, solid product is Ni, gaseous product is CO
2And water vapour; CO
2And water vapour overflows from the outlet of the fuel reaction device of heating, and condensation separation obtains purified CO after going out wherein water
2, realize CO
2Capture; The solid product Ni of the fuel reaction device of heating enters the air reactor bottom compartment in the fluidized-bed of heating by overflow groove, at the air reactor lower end of heating bubbling air, the air reactor bottom compartment of heating is in bubbling fluidization, and the temperature of the air reactor fluidized-bed of heating is controlled at 1000 ℃; The also Ni oxidation by air of ortho states generates NiO, discharges heat simultaneously; The air reactor transition section of NiO process heating and the air reactor riser tube of heating are to the air cyclonic separator of heating, gas-solid is through separating, air is overflowed from the air cyclonic separator outlet of heating, solid product NiO enters the fuel reaction device of heating through the air reactor tremie pipe of heating, and NiO realizes recycle.
Device technique scheme of the present invention is as follows:
A kind of hot coproduction of above-mentioned pair of circulation chain type hydrogen combusted and separation of C O of being used for
2The device of method, form by hydrogen generating system and heating; Hydrogen generating system is made up of air reactor fluidized-bed, fuel reaction device fluidized-bed, water vapour reactor fluidisation bed and first overflow groove; The air reactor fluidized-bed of hydrogen generating system is made up of air reactor bottom compartment, air reactor transition section, air reactor riser tube, air cyclonic separator, air reactor tremie pipe; The air reactor riser tube links to each other with the air reactor bottom compartment by the air reactor transition section, and the top of air reactor riser tube links to each other with the air cyclonic separator; The lower end of air cyclonic separator is the air reactor tremie pipe; The fuel reaction device fluidized-bed of hydrogen generating system adopts the fuel reaction device, and the air reactor tremie pipe inserts in the fuel reaction device; The water vapour reactor fluidisation bed of hydrogen generating system is by water vapour reactor bottom compartment, water vapour reactor transition section, and water vapour reactor riser, hydrogen cyclonic separator, water vapour reactor tremie pipe and water vapour reactor overflow groove are formed; The fuel reaction device of hydrogen generating system links to each other with the water vapour reactor bottom compartment of hydrogen generating system by first overflow groove; The water vapour reactor riser of hydrogen generating system links to each other with water vapour reactor bottom compartment by water vapour reactor transition section; The top of water vapour reactor riser links to each other with the hydrogen cyclonic separator; The hydrogen cyclonic separator links to each other with water vapour reactor overflow groove by water vapour reactor tremie pipe; Water vapour reactor overflow groove links to each other with the air reactor bottom compartment of hydrogen generating system; Heating is made up of fuel reaction device fluidized-bed, second overflow groove and air reactor fluidized-bed; The fuel reaction device fluidized-bed of heating is made up of fuel reaction device and fuel reaction device bottom air compartment and the fuel reaction device is positioned at the top of air compartment bottom the fuel reaction device; The fuel reaction device bottom air compartment of heating links to each other with the fuel reaction device exhanst gas outlet of hydrogen generating system by pipe connecting; The air reactor fluidized-bed of heating is made up of air reactor bottom compartment, air reactor transition section, air reactor riser tube, air cyclonic separator and air reactor tremie pipe; The air reactor riser tube of heating links to each other with the air reactor bottom compartment of heating by the air reactor transition section of heating; The top of the air reactor riser tube of heating links to each other with the air cyclonic separator of heating; The lower end of the air cyclonic separator of heating is the air reactor tremie pipe of heating; The air reactor tremie pipe of heating inserts in the fuel reaction device of heating; The fuel reaction device of heating links to each other with the air reactor bottom compartment of heating by second overflow groove.
Compared with prior art, the present invention has following advantage:
(1) ferric oxide Fe
2O
3As follows with nickel oxide NiO in the reaction process in the system separately:
Hydrogen generating system
Fe
2O
3In the fuel reaction device by for example synthetic gas or the Sweet natural gas reduction of carbonaceous geseous fuel:
3Fe
2O
3+H
2?2Fe
3O
4+H
2O （1）
3Fe
2O
3+CO?2Fe
3O
4+CO
2 （2）
12Fe
2O
3+CH
4?8Fe
3O
4+2H
2O+CO
2 （3）
Fe
3O
4+H
2?3FeO+H
2O （4）
Fe
3O
4+CO?3FeO+CO
2 （5）
4Fe
3O
4+CH
4?12FeO+2H
2O+CO
2 （6）
FeO+H
2?Fe+H
2O （7）
FeO+CO?Fe+CO
2 （8）
4FeO+CH
4?4Fe+2H
2O+CO
2 （9）
FeO and Fe react in the water vapour reactor and make hydrogen:
3FeO+H
2O?Fe
3O
4+H
2 （10）
3Fe+4H
2O?Fe
3O
4+4H
2 - （11）
Fe in air reactor
3O
4Obtain regeneration:
4Fe
3O
4+O
2?6Fe
2O
3 （12）
Heating:
NiO is in the reduction of fuel reaction device:
NiO+H
2?Ni+H
2O （13）
NiO+CO?Ni+CO
2 （14）
4NiO+CH
4?Ni+2H
2O+CO
2 （15）
The oxidizing reaction of Ni in air reactor:
2Ni+O
2?2NiO （16）
In hydrogen generating system, obtain hydrogen, ferric oxide Fe
2O
3Necessary drastic reduction is to FeO or Fe in the fuel reaction device.At Fe
2O
3Reduction process in, except at Fe
2O
3To Fe
3O
4Process in outside fuel gas can realize transforming fully, Fe
3O
4Reduction process to FeO and FeO to Fe is because the restriction of thermodynamic(al)equilibrium, and fuel gas can not be realized transforming fully, exports in the flue gas and must contain unconverted fuel gas H
2, CO or CH
4Simultaneously, at Fe
3O
4In the conversion process of FeO and Fe, the reduction reaction rate of ferriferous oxide and fuel gas is very slow on kinetics.So fuel reaction device middle outlet flue gas must contain unconverted H
2, CO and CH
4If this device has only in the hydrogen generating system flue gas that then the fuel reaction device is discharged and also has unreacted fuel, cause the total system energy conversion efficiency lowly to cause environmental pollution simultaneously.The flue gas of overflowing from hydrogen generating system fuel reaction device causes the fuel reaction device that heats reactor, because the thermodynamic behaviour of NiO and fuel reactant gas is different from Fe
2O
3, NiO and fuel reactant gas can be realized the conversion fully of fuel gas.The flue gas of the fuel reaction device of hydrogen generating system is introduced the fuel reaction device of heating, and unconverted fuel gas and NiO reaction obtain going back the Ni of ortho states, realize the conversion fully of fuel gas simultaneously, and the flue gas of the fuel reaction device discharge of heating only is CO
2And water vapour, condensation separation obtains purified carbonic acid gas after going out wherein water.Also the Ni of ortho states enters the air reactor of heating, with air calcination, produces a large amount of heats, and these heats can be by second stage employ, and the NiO after the regeneration enters the fuel reaction device and realizes recycle.By the ferriferous oxide circulation of hydrogen generating system and the nickel oxide circulation of heating, carbonaceous geseous fuel transforms for hydrogen, and has realized the separation of carbonic acid gas, has obtained heat simultaneously so respectively.Utilizing Aspen Plus chemical industry software simulation to calculate shows, when three reactor fluidisation bed apparatus of hydrogen generating system are only arranged, utilize ferriferous oxide as the round-robin oxygen carrier, be under 900 ℃ the condition at the fuel reaction device, the Carbon emission purity of the fuel reaction device outlet of hydrogen generating system has only 80%, utilize hydrogen generating system of the present invention to combine with heating, from the Carbon emission purity of heating outlet up to 99%.
(2) traditional coal gas hydrogen manufacturing is earlier gasification to be obtained with H
2With CO be the synthetic gas of main component, handle and the hydrogen of acquisition certain purity through purify, CO conversion and separating is purified etc. then.Compare with traditional gasification hydrogen manufacturing, the present invention is by water vapour and FeO and Fe reaction generation hydrogen, and gaseous product only can obtain purified hydrogen through the water that condensation separation goes out wherein, need not to relate to CO
2And H
2Separation, H
2The removing process of S and COS dusty gas reduces and realizes the related energy consumption of above technology.
(3) based on the principle of ferriferous oxide three reactor hydrogen manufacturing, adopt folded formula fluidized beds combustion reactor in theory also can realize the conversion fully of fuel gas, obtain to go back the FeO and the Fe of ortho states simultaneously, but folded formula fluidized beds combustion structure of reactor complexity, poor controllability, especially keep the material cycle stability relatively poor, cause it not necessarily can realize the conversion fully of fuel gas like this.In hydrogen manufacturing of the present invention and heating, the fuel reaction device has adopted the bubbling bed, controllability is good, fuel gas transforms owing to thermodynamic(al)equilibrium can only realize the part of fuel at the fuel reaction device of hydrogen generating system, and the flue gas that contains unconverted fuel gas has entered the fuel reaction device of heating, reduction NiO, realized that fuel gas transforms fully, final smoke components of discharging total system only is carbonic acid gas and water vapour, and condensation obtains purified carbonic acid gas after going out wherein water; Also the Ni of ortho states enters the air reactor calcining, discharges heat, and these heats can be by second stage employ.
Description of drawings
Fig. 1 is two hot coproduction of circulation chain type hydrogen combusted of the present invention and separation of C O
2Setting drawing.
Embodiment
Embodiment 1
Iron is placed the air reactor fluidized-bed 1 of hydrogen generating system I, and at the air reactor fluidized-bed lower end of hydrogen generating system I a bubbling air, the 1-1 of air reactor bottom compartment of hydrogen generating system I is in bubbling fluidization; The temperature of the air reactor fluidized-bed 1 of hydrogen generating system I is controlled at 1000 ℃; Iron and airborne oxygen reaction generate Fe
2O
3Fe
2O
3Through the air reactor transition section 1-2 of hydrogen generating system I and the air reactor riser tube 1-3 of hydrogen generating system I, by the air cyclonic separator 1-4 of air-lift unit to hydrogen generating system I, through gas solid separation, Fe
2O
3Air reactor tremie pipe 1-5 by hydrogen generating system I enters among the fuel reaction device 4-1 of hydrogen generating system I; The temperature of the fuel reaction device 4-1 of hydrogen generating system is controlled at 900 ℃; The fuel reaction device fluidized-bed lower end f of hydrogen generating system I feeds carbonaceous fuel gas, and the fuel reaction device 4-1 of hydrogen generating system I is in bubbling fluidization, Fe
2O
3Be reduced to FeO or Fe; FeO or Fe enter the water vapour reactor fluidisation bed 2 of hydrogen generating system I through overflow groove 3; Water vapour reactor fluidisation bed lower end d at hydrogen generating system I feeds water vapour, and the water vapour reactor 2-1 of bottom compartment is in bubbling fluidization, and the temperature of the water vapour reactor fluidisation bed 2 of hydrogen generating system I is controlled at 650 ℃; The also FeO of ortho states or Fe and water vapour reaction, solid product is Fe
3O
4, gaseous product is H
2Fe
3O
4Process water vapour reactor transition section 2-2 and water vapour reactor riser 2-3 are to hydrogen cyclonic separator 2-4, and gas-solid is through separating solid product Fe
3O
4Enter the air reactor fluidized-bed 1 of hydrogen generating system I through water vapour reactor tremie pipe 2-5 and water vapour reactor overflow groove 2-6, gaseous product is then overflowed through hydrogen cyclonic separator outlet c, and condensation separation obtains purified H after going out wherein water
2Enter the Fe of the air reactor fluidized-bed 1 of hydrogen generating system I
3O
4With air calcination, Fe
3O
4Be converted into Fe
2O
3, Fe
2O
3Realize recycle; The flue gas that comes out from the fuel reaction device 4-1 of hydrogen generating system I enters the fuel reaction device bottom air compartment 6-2 the fuel reaction device fluidized-bed 6 of heating II by pipe connecting 5; Add NiO in the fuel reaction device fluidized-bed 6 of heating II, the fuel reaction device 6-1 in the fuel reaction device fluidized-bed 6 is in bubbling fluidization; The temperature of the fuel reaction device 6-1 of heating II is controlled at 900 ℃; NiO with from the residual fuel gas reaction in the fuel reaction device 4-1 flue gas of hydrogen generating system I, solid product is Ni, gaseous product is CO
2And water vapour; CO
2And water vapour overflows from the fuel reaction device of heating II outlet k, and condensation separation obtains purified CO after going out wherein water
2, realize CO
2Capture; The solid product Ni of the fuel reaction device of heating II enters the 8-1 of air reactor bottom compartment in the fluidized-bed of heating II by overflow groove 7, at the air reactor lower end of heating II i bubbling air, the 8-1 of air reactor bottom compartment of heating II is in bubbling fluidization, and the temperature of the air reactor fluidized-bed 8 of heating II is controlled at 1000 ℃; The also Ni oxidation by air of ortho states generates NiO, discharges heat simultaneously; The air reactor transition section 8-2 of NiO process heating II and the air reactor riser tube 8-3 of heating II are to the air cyclonic separator 8-4 of heating II, gas-solid is through separating, air is overflowed from the air cyclonic separator outlet j of heating II, the air reactor tremie pipe 8-5 of solid product NiO process heating II enters the fuel reaction device 6-1 of heating II, and NiO realizes recycle; As accompanying drawing 1; The bottom b of the bottom h of the bottom e of first overflow groove 3, second overflow groove 7 and water vapour reactor overflow groove 2-6 feeds water vapour as loosening wind.
Embodiment 2
A kind ofly be used to realize hot coproduction of described pair of circulation chain type of claim 1 hydrogen combusted and separation of C O
2The device of method, form by hydrogen generating system I and heating II; Hydrogen generating system I is made up of air reactor fluidized-bed 1, fuel reaction device fluidized-bed 4, water vapour reactor fluidisation bed 2 and first overflow groove 3; The air reactor fluidized-bed 1 of hydrogen generating system I is made up of the 1-1 of air reactor bottom compartment, air reactor transition section 1-2, air reactor riser tube 1-3, air cyclonic separator 1-4, air reactor tremie pipe 1-5; Air reactor riser tube 1-3 links to each other with the 1-1 of air reactor bottom compartment by air reactor transition section 1-2, and the top of air reactor riser tube 1-3 links to each other with air cyclonic separator 1-4; The lower end of air cyclonic separator 1-4 is air reactor tremie pipe 1-5; The fuel reaction device fluidized-bed 4 of hydrogen generating system I adopts fuel reaction device 4-1, and air reactor tremie pipe 1-5 inserts in the fuel reaction device 4-1; The water vapour reactor fluidisation bed 2 of hydrogen generating system I is by the water vapour reactor 2-1 of bottom compartment, water vapour reactor transition section 2-2, water vapour reactor riser 2-3, hydrogen cyclonic separator 2-4, water vapour reactor tremie pipe 2-5 and water vapour reactor overflow groove 2-6 form; The fuel reaction device 4-1 of hydrogen generating system I links to each other with the water vapour reactor 2-1 of bottom compartment of hydrogen generating system I by first overflow groove 3; The water vapour reactor riser 2-3 of hydrogen generating system I links to each other with the water vapour reactor 2-1 of bottom compartment by water vapour reactor transition section 2-2; The top of water vapour reactor riser 2-3 links to each other with hydrogen cyclonic separator 2-4; Hydrogen cyclonic separator 2-4 links to each other with water vapour reactor overflow groove 2-6 by water vapour reactor tremie pipe 2-5; Water vapour reactor overflow groove 2-6 links to each other with the 1-1 of air reactor bottom compartment of hydrogen generating system I; Heating II is made up of fuel reaction device fluidized-bed 6, second overflow groove 7 and air reactor fluidized-bed 8; The fuel reaction device fluidized-bed 6 of heating II is made up of fuel reaction device 6-1 and fuel reaction device bottom air compartment 6-2 and fuel reaction device 6-1 is positioned at the top of air compartment 6-2 bottom the fuel reaction device; The fuel reaction device bottom air compartment 6-2 of heating II links to each other with the fuel reaction device 4-1 exhanst gas outlet of hydrogen generating system I by pipe connecting 5; The air reactor fluidized-bed 8 of heating II is made up of the 8-1 of air reactor bottom compartment, air reactor transition section 8-2, air reactor riser tube 8-3, air cyclonic separator 8-4 and air reactor tremie pipe 8-5; The air reactor riser tube 8-3 of heating II links to each other with the 8-1 of air reactor bottom compartment of heating II by the air reactor transition section 8-2 of heating II; The top of the air reactor riser tube 8-3 of heating II links to each other with the air cyclonic separator 8-4 of heating II; The lower end of the air cyclonic separator 8-4 of heating II is the air reactor tremie pipe 8-5 of heating II; The air reactor tremie pipe 8-5 of heating II inserts in the fuel reaction device 6-1 of heating II; The fuel reaction device 6-1 of heating II links to each other with the 8-1 of air reactor bottom compartment of heating II by second overflow groove 7; As accompanying drawing 1.
Claims (4)
1. two hot coproduction of circulation chain type hydrogen combusted and separation of C O
2Method, it is characterized in that: the air reactor fluidized-bed (1) that iron is placed hydrogen generating system (I), at the air reactor fluidized-bed lower end (a) of hydrogen generating system (I) bubbling air, the air reactor bottom compartment (1-1) of hydrogen generating system (I) is in bubbling fluidization; The temperature of the air reactor fluidized-bed (1) of hydrogen generating system (I) is controlled at 1000 ℃; Iron and airborne oxygen reaction generate Fe
2O
3Fe
2O
3Through the air reactor transition section (1-2) of hydrogen generating system (I) and the air reactor riser tube (1-3) of hydrogen generating system (I), by the air cyclonic separator (1-4) of air-lift unit to hydrogen generating system (I), through gas solid separation, Fe
2O
3Air reactor tremie pipe (1-5) by hydrogen generating system (I) enters in the fuel reaction device (4-1) of hydrogen generating system (I); The temperature of the fuel reaction device (4-1) of hydrogen generating system is controlled at 900 ℃; The fuel reaction device fluidized-bed lower end (f) of hydrogen generating system (I) feeds carbonaceous fuel gas, and the fuel reaction device (4-1) of hydrogen generating system (I) is in bubbling fluidization, Fe
2O
3Be reduced to FeO or Fe; FeO or Fe enter the water vapour reactor fluidisation bed (2) of hydrogen generating system (I) through overflow groove (3); Water vapour reactor fluidisation bed lower end (d) at hydrogen generating system (I) feeds water vapour, and water vapour reactor bottom compartment (2-1) is in bubbling fluidization, and the temperature of the water vapour reactor fluidisation bed (2) of hydrogen generating system (I) is controlled at 650 ℃; The also FeO of ortho states or Fe and water vapour reaction, solid product is Fe
3O
4, gaseous product is H
2Fe
3O
4Process water vapour reactor transition section (2-2) and water vapour reactor riser (2-3) are to hydrogen cyclonic separator (2-4), and gas-solid is through separating solid product Fe
3O
4Process water vapour reactor tremie pipe (2-5) and water vapour reactor overflow groove (2-6) enter the air reactor fluidized-bed (1) of hydrogen generating system (I), gaseous product is then overflowed through hydrogen cyclonic separator outlet (c), condensation separation obtains purified H after going out wherein water
2Enter the Fe of the air reactor fluidized-bed (1) of hydrogen generating system (I)
3O
4With air calcination, Fe
3O
4Be converted into Fe
2O
3, Fe
2O
3Realize recycle; The flue gas that comes out from the fuel reaction device (4-1) of hydrogen generating system (I) enters the fuel reaction device bottom air compartment (6-2) the fuel reaction device fluidized-bed (6) of heating (II) by pipe connecting (5); Add NiO in the fuel reaction device fluidized-bed (6) of heating (II), the fuel reaction device (6-1) in the fuel reaction device fluidized-bed (6) is in bubbling fluidization; The temperature of the fuel reaction device (6-1) of heating (II) is controlled at 900 ℃; NiO with from the residual fuel gas reaction in fuel reaction device (4-1) flue gas of hydrogen generating system (I), solid product is Ni, gaseous product is CO
2And water vapour; CO
2And water vapour overflows from the fuel reaction device of heating (II) outlet (k), and condensation separation obtains purified CO after going out wherein water
2, realize CO
2Capture; The solid product Ni of the fuel reaction device of heating (II) enters the air reactor bottom compartment (8-1) in the fluidized-bed of heating (II) by overflow groove (7), at the air reactor lower end of heating (II) (i) bubbling air, the air reactor bottom compartment (8-1) of heating (II) is in bubbling fluidization, and the temperature of the air reactor fluidized-bed (8) of heating (II) is controlled at 1000 ℃; The also Ni oxidation by air of ortho states generates NiO, discharges heat simultaneously; The air reactor transition section (8-2) of NiO process heating (II) and the air reactor riser tube (8-3) of heating (II) are to the air cyclonic separator (8-4) of heating (II), gas-solid is through separating, air is overflowed from the air cyclonic separator outlet (j) of heating (II), solid product NiO enters the fuel reaction device (6-1) of heating (II) through the air reactor tremie pipe (8-5) of heating (II), and NiO realizes recycle.
2. hot coproduction of according to claim 1 pair of circulation chain type hydrogen combusted and separation of C O
2Method, it is characterized in that hydrogen generating system (I) round-robin material is Fe
2O
3, FeO, Fe and Fe
3O
4Heating (II) round-robin material is NiO and Ni.
3. one kind is used to realize hot coproduction of described pair of circulation chain type of claim 1 hydrogen combusted and separation of C O
2The device of method, it is characterized in that, form by hydrogen generating system (I) and heating (II); Hydrogen generating system (I) is made up of air reactor fluidized-bed (1), fuel reaction device fluidized-bed (4), water vapour reactor fluidisation bed (2) and first overflow groove (3); The air reactor fluidized-bed (1) of hydrogen generating system (I) is made up of air reactor bottom compartment (1-1), air reactor transition section (1-2), air reactor riser tube (1-3), air cyclonic separator (1-4), air reactor tremie pipe (1-5); Air reactor riser tube (1-3) links to each other with air reactor bottom compartment (1-1) by air reactor transition section (1-2), and the top of air reactor riser tube (1-3) links to each other with air cyclonic separator (1-4); The lower end of air cyclonic separator (1-4) is air reactor tremie pipe (1-5); The fuel reaction device fluidized-bed (4) of hydrogen generating system (I) adopts fuel reaction device (4-1), and air reactor tremie pipe (1-5) inserts in the fuel reaction device (4-1); The water vapour reactor fluidisation bed (2) of hydrogen generating system (I) is by water vapour reactor bottom compartment (2-1), water vapour reactor transition section (2-2), water vapour reactor riser (2-3), hydrogen cyclonic separator (2-4), water vapour reactor tremie pipe (2-5) and water vapour reactor overflow groove (2-6) are formed; The fuel reaction device (4-1) of hydrogen generating system (I) links to each other with the water vapour reactor bottom compartment (2-1) of hydrogen generating system (I) by first overflow groove (3); The water vapour reactor riser (2-3) of hydrogen generating system (I) links to each other with water vapour reactor bottom compartment (2-1) by water vapour reactor transition section (2-2); The top of water vapour reactor riser (2-3) links to each other with hydrogen cyclonic separator (2-4); Hydrogen cyclonic separator (2-4) links to each other with water vapour reactor overflow groove (2-6) by water vapour reactor tremie pipe (2-5); Water vapour reactor overflow groove (2-6) links to each other with the air reactor bottom compartment (1-1) of hydrogen generating system (I); Heating (II) is made up of fuel reaction device fluidized-bed (6), second overflow groove (7) and air reactor fluidized-bed (8); The fuel reaction device fluidized-bed (6) of heating (II) is made up of fuel reaction device (6-1) and fuel reaction device bottom air compartment (6-2) and fuel reaction device (6-1) is positioned at the top of air compartment (6-2) bottom the fuel reaction device; The fuel reaction device bottom air compartment (6-2) of heating (II) links to each other with fuel reaction device (4-1) exhanst gas outlet of hydrogen generating system (I) by pipe connecting (5); The air reactor fluidized-bed (8) of heating (II) is made up of air reactor bottom compartment (8-1), air reactor transition section (8-2), air reactor riser tube (8-3), air cyclonic separator (8-4) and air reactor tremie pipe (8-5); The air reactor riser tube (8-3) of heating (II) links to each other with the air reactor bottom compartment (8-1) of heating (II) by the air reactor transition section (8-2) of heating (II); The top of the air reactor riser tube (8-3) of heating (II) links to each other with the air cyclonic separator (8-4) of heating (II); The lower end of the air cyclonic separator (8-4) of heating (II) is the air reactor tremie pipe (8-5) of heating (II); The air reactor tremie pipe (8-5) of heating (II) inserts in the fuel reaction device (6-1) of heating (II); The fuel reaction device (6-1) of heating (II) links to each other with the air reactor bottom compartment (8-1) of heating (II) by second overflow groove (7).
4. device according to claim 3 is characterized in that, the bottom (e) of first overflow groove (3), the bottom (h) of second overflow groove (7) feed water vapour as loosening wind with the bottom (b) of water vapour reactor overflow groove (2-6).
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