A method of producing hydrogen

Abstract

The application discloses a hydrogen production method, which comprises the following steps: water vapor is subjected to magnetization treatment, and then enters a steam reactor to react with a reducing-state oxygen carrier entering from the top of the steam reactor, so that hydrogen and an oxidizing-state oxygen carrier are obtained; the hydrogen and unreacted water vapor flow out from the upper part of the steam reactor, and hydrogen is obtained after separation; and the oxidizing-state oxygen carrier is discharged from the bottom of the reactor and recycled to the steam reactor after reduction. The method can significantly improve the yield of chemical ring hydrogen production.

Description

TECHNICAL FIELD

[0001] The present application relates to a hydrogen production method, in particular to a hydrogen production method by steam reduction reaction. BACKGROUND

[0002] Chemical looping hydrogen production is a hydrogen production technology with industrialization prospect, which is a new technology of hydrogen production and carbon dioxide capture. It divides the natural gas steam reforming reaction into three steps, and obtains hydrogen and carbon dioxide in two reactors respectively, without gas separation, with the advantages of high hydrogen production efficiency, high hydrogen purity and zero carbon dioxide emission, which is very suitable for the development requirements of current and future hydrogen production technology. After more than ten years of research and development, the United States has built the world's first industrialization demonstration device, and is getting closer to industrialization application. Considering energy, resources and environment, natural gas is the best choice as the fuel for chemical looping hydrogen production, but its economic efficiency needs to be improved.

[0003] CN201610457306.9 provides a process device and method for chemical looping hydrogen production, which includes two fuel reactors, a steam reactor and an air reactor. The gas outlet of the fuel reactor I is connected with the gas inlet of the fuel reactor II, the oxygen carrier outlets of the two fuel reactors are connected with the oxygen carrier inlets of the steam reactor, and the steam reactor is connected with the air reactor. By using the above process device, the reaction temperature in the fuel reactor I is controlled at 750-800℃, the reaction temperature in the fuel reactor II is controlled at 650-750℃, the reaction of fuel gas in the fuel reactor is divided into two stages, the reaction temperature is greatly reduced compared with the general process condition (850-950℃), the energy consumption is reduced, the conversion of fuel gas to carbon dioxide is more complete, and the CH4 conversion rate and CO2 selectivity are improved.

[0004] CN201010118131.1 combines biomass gasification hydrogen production with chemical looping combustion to realize low-cost carbon dioxide separation; metal oxides are used as heat carriers and oxygen carriers to circulate between three beds to realize the staged utilization of matter and energy. The system mainly includes an air reactor, a fuel reactor, a moving bed gasification furnace, a gas-solid separation device, a gas purification device, a hydrogen separation device and a subsequent utilization device. The system can realize hydrogen production and CO2 near-zero emission hydrogen production, thereby realizing efficient and clean utilization of biomass.

[0005] CN201610209319.4 discloses a switching type chemical chain hydrogen production device, comprising at least three chemical chain reactors and at least two CaO reactors connected in parallel, each chemical chain reactor is respectively provided with five inlets and five outlets, and each CaO reactor is respectively provided with one inlet and two outlets, the inlets and outlets are connected with different gas pipelines through valves. The device can realize hydrogen production through the reduction and oxidation cycle of oxygen carriers, divide the reaction into three reaction stages with the same reaction time, and control each chemical chain reactor to be in different stages, so that the cycle and continuous production of hydrogen production are realized. The device realizes the immobilized reaction of oxygen carriers, avoids the wear caused by the flow of oxygen carriers in the reactors, and improves the utilization rate of oxygen carriers; the device is designed ingeniously, realizes continuous production, and improves the utilization rate of the reactors.

[0006] CN201610499615.2 discloses a device and method for preparing high-purity hydrogen by biomass pyrolysis-chemical chain combustion, comprising a biomass pyrolysis unit, a chemical chain hydrogen production unit and a waste heat recovery unit. The biomass pyrolysis unit comprises a vertical silo, a screw feeder, a rotary kiln pyrolysis reactor and a high-temperature filter. The chemical chain hydrogen production unit comprises an air inlet end gas path switching system, at least one fixed bed reactor and an air outlet end gas path switching system, wherein the fixed bed reactor is composed of three parallel fixed bed reactors I, II and III, which successively and continuously undergo fuel reduction-steam oxidation-air combustion stages (steam blowing stages). The waste heat recovery unit comprises a waste heat boiler, a cooler and a gas-liquid separator. The process flow for preparing hydrogen from biomass is short, the hydrogen-containing product obtained by introducing the pyrolysis gas into the chemical chain hydrogen production unit can obtain high-purity hydrogen after simple condensation and water removal, there is no complex gas purification device, and the hydrogen production cost is low.

[0007] CN201610128875.9 discloses a chemical chain hydrogen production device and method based on metal oxygen carriers, which can realize the preparation of high-purity hydrogen and achieve the effect of internal separation of carbon dioxide. The device comprises an air reactor, a cyclone separator, a first fuel reactor, a second fuel reactor, a gasification reactor and an isolator. The method is that the reduced oxygen carriers in the air reactor are oxidized by air to generate oxidized oxygen carriers, the oxidized oxygen carriers are separated from the gas by the cyclone separator, and the oxidized oxygen carrier particles enter the first fuel reactor; the oxygen carriers in the first fuel reactor are reduced by fuel gas to generate reduced oxygen carriers; the oxygen carriers in the first fuel reactor are further reduced by fuel gas in the second fuel reactor and enter the gasification reactor through the second fuel reactor; the reduced oxygen carriers in the gasification reactor perform hydrogen production reaction with steam to generate hydrogen and reduced oxygen carriers; and the reduced oxygen carriers in the gasification reactor return to the air reactor through the isolator.

[0008] CN201610209320.7 discloses an integrated switching chemical chain hydrogen production device, which comprises an integrated chemical chain reactor and two CaO reactors. The integrated chemical chain reactor is internally divided into three reactors, each of which is respectively provided with five inlets and five outlets. The CaO reactors are respectively provided with one inlet and two outlets. The inlets and outlets are connected with different gas pipelines through valves. The device can realize hydrogen production through the reduction and oxidation cycle of the oxygen carrier, and the reaction is divided into three reaction stages with the same reaction time. The three reactors in the integrated chemical chain reactor are controlled to be in different stages, thereby realizing the cycle and continuous production of hydrogen production. The device realizes the immobilized reaction of the oxygen carrier, avoids the wear caused by the flow of the oxygen carrier in each reactor, and improves the utilization rate of the oxygen carrier. The device is designed ingeniously, the heat transfer between the reactors is enhanced, and continuous production is realized.

[0009] CN201610499611.4 discloses an iron-based oxygen carrier deep reduction chemical chain hydrogen production device and method. The device comprises a gas path switching system at the inlet, four fixed bed reactors arranged in sequence, and a gas path switching system at the tail gas end. Two fixed bed reactors are in the reduction stage. Under the premise of ensuring complete combustion of the fuel, the solid phase conversion rate of the iron-based oxygen carrier is improved. The four fixed bed reactors are in the fuel reduction, deep reduction, steam oxidation and air combustion stages (steam sweeping stage) in turn, thereby realizing a continuous and efficient chemical chain hydrogen production process. In the present application, the reduction solid phase conversion rate of the iron-based oxygen carrier is greatly improved, the hydrogen production intensity per unit of oxygen carrier is significantly increased, and the hydrogen production efficiency of the device is effectively improved. High-purity hydrogen is obtained without complex gas purification devices, and the cost of hydrogen production is reduced.

[0010] CN201820266134.1 discloses a fuel chemical chain hydrogen production system, which comprises two identical chemical chain combustion reactors. Each chemical chain combustion reactor comprises an outer pipe and an inner pipe coaxially arranged in the outer pipe. The inner pipe is filled with a first oxygen carrier, and the interlayer between the outer pipe and the inner pipe is filled with a second oxygen carrier. The upper end of the inner pipe is connected with a water vapor introduction pipeline and a fuel introduction pipeline, and the lower end of the inner pipe is connected with a gas outlet pipeline. When the first chemical chain combustion reactor introduces water vapor to perform an oxygen carrier oxidation reaction with the reduced oxygen carrier, the second chemical chain combustion reactor introduces fuel to perform an oxygen carrier reduction reaction with the oxidized oxygen carrier. The fuel chemical chain hydrogen production system has simple process, compact reactor and easy miniaturization, and can efficiently produce pure hydrogen from gaseous or liquid fuel.

[0011] In summary, the chemical loop hydrogen production technology has made significant progress, but the hydrogen production efficiency still needs to be further improved. SUMMARY

[0012] In order to solve the problem of low hydrogen production efficiency in the chemical looping hydrogen production process in the prior art, the application provides a hydrogen production method, which can significantly improve the yield of chemical looping hydrogen production.

[0013] A method for producing hydrogen, the method comprising the following steps: water vapor is subjected to magnetization treatment and then enters a steam reactor to react with a reduced oxygen carrier entering from the top of the steam reactor, so as to obtain hydrogen and an oxidized oxygen carrier; the hydrogen and unreacted water vapor flow out from the upper part of the steam reactor, and hydrogen is obtained after separation; and the oxidized oxygen carrier is discharged from the bottom of the reactor and then recycled to the steam reactor after reduction.

[0014] In the above method, the water vapor can be obtained by vaporizing liquid water, for example, in the form of evaporation or boiling, preferably in the form of evaporation, and further preferably in the form of multi-stage evaporation.

[0015] In the above method, the water vapor is subjected to magnetization treatment and then enters the steam reactor, for example, the water vapor enters the steam reactor after passing through a magnetizer, and the magnetic induction intensity of the magnetic field of the magnetizer is 1000-5000 GS, preferably 1200-4000 GS, and further preferably 1500-3000 GS.

[0016] In the above method, the active center of the oxygen carrier is one or more of copper oxide, nickel oxide, manganese oxide, diiron trioxide, tricobalt tetroxide, titanium oxide and calcium sulfate; preferably one or more of copper oxide, diiron trioxide, titanium oxide and calcium sulfate; and further preferably one or more of copper oxide, diiron trioxide and titanium oxide. The active center of the oxygen carrier can be supported on a carrier.

[0017] In the above method, the reaction conditions of the steam reactor are as follows: the reaction temperature is 600-1000℃, preferably 650-800℃; the water vapor space velocity is 300-3000 h -1 , preferably 500-2000 h -1 , the flow speed of the oxygen carrier is 20g / min-200g / min, preferably 50g / min-150g / min.

[0018] In the above method, the oxidized oxygen carrier is contacted with a reducing gas in a fuel reactor to produce a reduced oxygen carrier. Preferably, the oxidized oxygen carrier is contacted with oxygen in an air reactor to perform a deep oxidation reaction, and then contacted with a reducing gas in a fuel reactor to produce a reduced oxygen carrier. The reducing gas includes CO, CH4 or H2, and preferably is methane. The reaction conditions of the fuel reactor are as follows: the reactor temperature is 600-1000°C, preferably 750-900°C; the reducing gas space velocity is 500-2000 h -1 The oxygen can be derived from an oxygen-containing gas, typically air. The reaction conditions of the air reactor are as follows: the reaction temperature is 600-1000°C, preferably 700-800°C; the air space velocity is 1000-10000 h -1 .

[0019] A specific method for producing hydrogen, comprising the following steps:

[0020] (1) water vapor after magnetization is introduced into a steam reactor to contact with a reduced oxygen carrier introduced into the steam reactor from the top to perform a reaction, to obtain hydrogen and an oxidized oxygen carrier; the hydrogen and unreacted water vapor are introduced into the upper part of the steam reactor, and after separation, hydrogen is obtained;

[0021] (2) the oxidized oxygen carrier obtained in step (1) is contacted with oxygen in an air reactor to perform a deep oxidation reaction;

[0022] (3) the oxygen carrier after deep oxidation in step (2) is contacted with a reducing gas in a fuel reactor to produce a reduced oxygen carrier, which is recycled to the steam reactor in step (1) to contact with water vapor after magnetization to perform a reaction.

[0023] In step (1) of the above method, the water vapor can be obtained by vaporizing liquid water, such as by evaporation or boiling, preferably by evaporation, and further preferably by multi-stage evaporation.

[0024] In step (1) of the above method, the water vapor after magnetization is introduced into the steam reactor, specifically, the water vapor is introduced into the steam reactor after passing through a magnetizer, and the magnetic induction intensity of the magnetic field of the magnetizer is 1000-5000 GS, preferably 1200-4000 GS, and further preferably 1500-3000 GS. For example, the water vapor is introduced into the steam reactor after passing through a magnetization tube to contact with the reduced oxygen carrier introduced into the steam reactor from the top to perform a reaction.

[0025] In the step (1) of the method, the active center of the oxygen carrier is one or more of copper oxide, nickel oxide, manganese oxide, ferric oxide, cobalt trioxide, titanium oxide and calcium sulfate; preferably one or more of copper oxide, ferric oxide, titanium oxide and calcium sulfate; and more preferably one or more of copper oxide, ferric oxide and titanium oxide. The active center of the oxygen carrier can be loaded on a carrier. The carrier is SiO2, Al2O3, MgO-SiO2, MgO-Al2O3, Al2O3-SiO2, CaO-SiO2, CaO-MgO-SiO2 or a combination thereof, preferably SiO2, Al2O3, MgO-SiO2, MgO-Al2O3 or a combination thereof.

[0026] In the step (1) of the method, the oxygen carrier contains CeFe 20 Ti 10 O5 composite oxide and Al2O3, and the content of the CeFe 20 Ti 10 O5 composite oxide is 40%-60% based on the weight of the oxygen carrier.

[0027] In the step (1) of the method, the reaction conditions of the steam reactor are as follows: the reaction temperature is 600-1000℃, preferably 650-800℃; and the water vapor space velocity is 300-3000 h -1 , preferably 500-2000 h -1 .

[0028] In the step (2) of the method, the oxygen can be derived from an oxygen-containing gas, which is generally air, and the reaction conditions of the air reactor are as follows: the reaction temperature is 600-1000℃, preferably 700-800℃; and the air space velocity is 1000-10000 h -1 .

[0029] In the step (3) of the method, the reducing gas includes CO, CH4 or H2, and is preferably methane. The reaction conditions of the fuel reactor are as follows: the reactor temperature is 600-1000℃, preferably 750-900℃; and the reducing gas space velocity is 500-2000 h -1 .

[0030] The inventors have found through in-depth research that water vapor changes its physical and chemical properties under the action of a magnetic field of a certain intensity after being subjected to magnetic treatment. The water vapor subjected to magnetic treatment causes self-polarization, increases its polarity, changes the outer electron cloud distribution of the molecules and ions, cuts the original long associated molecular chains into short associated molecular chains, changes the physical properties of the water vapor, and increases the electrical conductivity, light transmission coefficient, surface tension, activity and osmotic pressure.

[0031] Compared with the prior art, the hydrogen production method has the following advantages: the hydrogen production method of the present application magnetizes the water vapor raw material at the feed inlet of the steam reactor, changes the physicochemical properties of the water vapor, reduces the latent heat of vaporization of water, improves the activity of the water vapor and the single-pass conversion rate of hydrogen, and reduces energy consumption. DETAILED DESCRIPTION

[0032] The effects and advantages of the method of the present application will be further illustrated below in combination with examples and comparative examples, but the following examples do not constitute a limitation on the method of the present application. In the context of the present application, unless otherwise specified, all are mass percentages.

[0033] The composition and content of the oxygen carrier used in the examples and comparative examples of the present application are as follows: the active center composite oxide has a composition of CeFe 20 Ti 10 O5The composite oxide and Al2O3 are uniformly mixed in a mass ratio of 1:1, extruded into a strip, dried, and then calcined at a drying temperature of 100°C for 24 hours and a calcination temperature of 1000°C for 10 hours. The calculation method of hydrogen production is the volume of hydrogen at normal temperature and pressure after cooling divided by the mass of the oxygen carrier.

[0034] Example 1

[0035] The air compressor is turned on to adjust the air mass flow meter, and the oxygen carrier moving speed controller is turned on. After the solid circulation of the system is stable, the temperature is raised to the reaction temperature. After the temperature is stable, the combustion gas is introduced into the combustion reactor, and the raw water of the steam reactor is preheated and then introduced into the steam reactor. The tail gas of the steam reactor is collected for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 1500GS; the reaction temperature of the water vapor reactor is 650°C, the space velocity of the water vapor is 500h -1 ; the operating temperature of the air reactor is 700°C, and the space velocity of the air is 1000h -1 ; the operating temperature of the combustion reactor is 750°C, and the space velocity of the reducing gas is 500h -1 ; and the flow speed of the oxygen carrier is 50g / min. After 24 hours of reaction, the tail gas of the steam reactor is collected for composition analysis.

[0036] Example 2

[0037] The air compressor is turned on to adjust the air mass flow meter, and the oxygen carrier moving speed controller is turned on. After the solid circulation of the system is stable, the temperature is raised to the reaction temperature. After the temperature is stable, the combustion gas is introduced into the combustion reactor, and the raw water of the steam reactor is preheated and then introduced into the steam reactor. The tail gas of the steam reactor is collected for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 1500GS; the reaction temperature of the water vapor reactor is 650°C, the space velocity of the water vapor is 500h-1 ; air reactor operating temperature 800°C, air space velocity 10000h -1 ; combustion reactor operating temperature 900°C, reducing gas space velocity 2000h -1 Oxygen carrier flow rate 150g / min. After 24 hours of reaction, the steam reactor tail gas was collected for composition analysis.

[0038] Example 3

[0039] The air compressor was turned on to adjust the air mass flow meter, and the oxygen carrier moving speed controller was turned on. After the solid circulation of the system was stable, the temperature was raised to the reaction temperature. After the temperature was stable, the combustion gas was introduced into the combustion reactor, and the raw water of the steam reactor was preheated and then introduced into the steam reactor. The steam reactor tail gas was collected for composition analysis. The magnetic field set by the magnetizer had a magnetic induction intensity of 2000GS; the water vapor reactor reaction temperature was 700°C, and the water vapor space velocity was 1000h -1 ; air reactor operating temperature 750°C, air space velocity 5000h -1 ; combustion reactor operating temperature 800°C, reducing gas space velocity 1000h -1 Oxygen carrier flow rate 100g / min. After 24 hours of reaction, the steam reactor tail gas was collected for composition analysis.

[0040] Example 4

[0041] The air compressor was turned on to adjust the air mass flow meter, and the oxygen carrier moving speed controller was turned on. After the solid circulation of the system was stable, the temperature was raised to the reaction temperature. After the temperature was stable, the combustion gas was introduced into the combustion reactor, and the raw water of the steam reactor was preheated and then introduced into the steam reactor. The steam reactor tail gas was collected for composition analysis. The magnetic field set by the magnetizer had a magnetic induction intensity of 2200GS; the water vapor reactor reaction temperature was 700°C, and the water vapor space velocity was 1000h -1 ; air reactor operating temperature 750°C, air space velocity 5000h -1 ; combustion reactor operating temperature 800°C, reducing gas space velocity 1000h -1 Oxygen carrier flow rate 80g / min. After 24 hours of reaction, the steam reactor tail gas was collected for composition analysis.

[0042] Example 5

[0043] Start the air compressor to adjust the air mass flow meter, open the oxygen carrier moving speed controller, after the system solid circulation is stable, increase the temperature to the reaction temperature, after the temperature is stable, introduce the combustion gas into the combustion reactor, and the raw water of the steam reactor enters the steam reactor after preheating. The tail gas of the steam reactor is collected for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 2000GS; the reaction temperature of the water vapor reactor is 800°C, the space velocity of the water vapor is 1200h -1 ; the operation temperature of the air reactor is 800°C, the space velocity of the air is 5000h -1 ; the operation temperature of the combustion reactor is 820°C, the space velocity of the reducing gas is 1200h -1 , and the flow speed of the oxygen carrier is 90g / min. After 24 hours of reaction, the tail gas of the steam reactor is collected for composition analysis.

[0044] Example 6

[0045] Start the air compressor to adjust the air mass flow meter, open the oxygen carrier moving speed controller, after the system solid circulation is stable, increase the temperature to the reaction temperature, after the temperature is stable, introduce the combustion gas into the combustion reactor, and the raw water of the steam reactor enters the steam reactor after preheating. The tail gas of the steam reactor is collected for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 2200GS; the reaction temperature of the water vapor reactor is 750°C, the space velocity of the water vapor is 1000h -1 ; the operation temperature of the air reactor is 800°C, the space velocity of the air is 5000h -1 ; the operation temperature of the combustion reactor is 800°C, the space velocity of the reducing gas is 1000h -1 , and the flow speed of the oxygen carrier is 100g / min. After 24 hours of reaction, the tail gas of the steam reactor is collected for composition analysis.

[0046] Example 7

[0047] Start the air compressor to adjust the air mass flow meter, open the oxygen carrier moving speed controller, after the system solid circulation is stable, increase the temperature to the reaction temperature, after the temperature is stable, introduce the combustion gas into the combustion reactor, and the raw water of the steam reactor enters the steam reactor after preheating. The tail gas of the steam reactor is collected for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 3000GS; the reaction temperature of the water vapor reactor is 700°C, the space velocity of the water vapor is 1000h -1 ; the operation temperature of the air reactor is 750°C, the space velocity of the air is 6000h -1 ; the operation temperature of the combustion reactor is 800°C, the space velocity of the reducing gas is 1500h -1 , and the flow speed of the oxygen carrier is 120g / min. After 24 hours of reaction, the tail gas of the steam reactor is collected for composition analysis.

[0048] Example 8

[0049] Start air compressor to adjust air mass flow meter, open the carrier oxygen body moving speed controller, after the system solid circulation is stable, temperature is raised to reaction temperature, after the temperature is stable, the combustion reactor is connected with combustion gas, the raw material water of steam reactor is preheated and then enters the steam reactor. Collect the tail gas of steam reactor for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 3000GS; the reaction temperature of water vapor reactor is 650℃, the space velocity of water vapor is 1200h -1 ; the operating temperature of air reactor is 750℃, the space velocity of air is 6000h -1 ; the operating temperature of combustion reactor is 800℃, the space velocity of reducing gas is 1500h -1 , the flow speed of carrier oxygen body is 70g / min. Collect the tail gas of steam reactor for composition analysis after 24 hours of reaction.

[0050] Example 9

[0051] Start air compressor to adjust air mass flow meter, open the carrier oxygen body moving speed controller, after the system solid circulation is stable, temperature is raised to reaction temperature, after the temperature is stable, the combustion reactor is connected with combustion gas, the raw material water of steam reactor is preheated and then enters the steam reactor. Collect the tail gas of steam reactor for composition analysis. The magnetic induction intensity of the magnetic field set by the magnetizer is 2500GS; the reaction temperature of water vapor reactor is 700℃, the space velocity of water vapor is 1500h -1 ; the operating temperature of air reactor is 750℃, the space velocity of air is 8000h -1 ; the operating temperature of combustion reactor is 800℃, the space velocity of reducing gas is 1200h -1 , the flow speed of carrier oxygen body is 60g / min. Collect the tail gas of steam reactor for composition analysis after 24 hours of reaction.

[0052] Comparative Example

[0053] Start air compressor to adjust air mass flow meter, open the carrier oxygen body moving speed controller, after the system solid circulation is stable, temperature is raised to reaction temperature, after the temperature is stable, the combustion reactor is connected with combustion gas, the raw material water of steam reactor is preheated and then enters the steam reactor. Collect the tail gas of steam reactor for composition analysis. The reaction temperature of water vapor reactor is 700℃, the space velocity of water vapor is 1000h -1 ; the operating temperature of air reactor is 750℃, the space velocity of air is 5000h -1 ; the operating temperature of combustion reactor is 800℃, the space velocity of reducing gas is 1000h -1 , the flow speed of carrier oxygen body is 100g / min. Collect the tail gas of steam reactor for composition analysis after 24 hours of reaction.

[0054] The reaction conditions and results of the above examples and comparative examples are shown in Table 1

[0055]

Claims

1. A method of producing hydrogen, characterized by: The method comprises the following steps: water vapor is subjected to magnetization treatment and then enters a steam reactor to react with a reduced oxygen carrier entering from the top of the steam reactor, so as to obtain hydrogen and an oxidized oxygen carrier; the hydrogen and unreacted water vapor flow out from the top of the steam reactor, and hydrogen is obtained after separation. The oxygen carrier in the oxidation state is discharged from the bottom of the reactor and recycled back to the steam reactor after reduction; the oxygen carrier contains CeFe 20 Ti 10 O5 composite oxide and Al2O3, based on the weight of the oxygen carrier CeFe 20 Ti 10 The content of the O5 composite oxide is 40wt%-60wt%.

2. The method of claim 1, wherein: The water vapor is obtained by vaporizing liquid water.

3. The method of claim 2, wherein: The water vapor is obtained by evaporation or boiling.

4. The method of claim 3, wherein: The water vapor is obtained by multi-stage evaporation.

5. The method of claim 1, wherein: The water vapor is subjected to magnetization treatment and then enters the steam reactor.

6. The method of claim 5, wherein: The magnetic induction intensity of the magnetic field of the magnetizer is 1000-5000 GS.

7. The method of claim 6, wherein: The magnetic induction intensity of the magnetic field of the magnetizer is 1200-4000 GS.

8. The method of claim 6, wherein: The magnetic induction intensity of the magnetic field of the magnetizer is 1500-3000 GS.

9. The method of claim 1, wherein: The water vapor enters the steam reactor after passing through a magnetization tube to react with the reduced oxygen carrier entering from the top of the steam reactor.

10. The method of claim 1, wherein: The reaction conditions of the steam reactor are as follows: the reaction temperature is 600-1000℃, the water vapor volume space velocity is 300-3000h -1 , and the oxygen carrier flow speed is 20g / min-200g / min.

11. The method of claim 10, wherein: The reaction conditions of the steam reactor are as follows: the reaction temperature is 650-800℃, the water vapor volume space velocity is 500-2000h -1 , and the oxygen carrier flow speed is 50g / min-150g / min.

12. The method of claim 1, wherein: The oxidized oxygen carrier is contacted with a reducing gas in a fuel reactor to obtain the reduced oxygen carrier.

13. The method of claim 12, wherein: The oxidized oxygen carrier is subjected to deep oxidation reaction with oxygen in an air reactor and then is contacted with a reducing gas in a fuel reactor to obtain the reduced oxygen carrier.

14. The method of claim 12, wherein: The reducing gas comprises CO, CH4 or H2.

15. The method of claim 12, wherein: The reaction conditions of the fuel reactor are as follows: the reactor temperature is 600-1000℃, the reducing gas space velocity is 500-2000h -1 .

16. The method of claim 15, wherein: The reactor temperature of the fuel reactor is 750-900 ℃.

17. The method of claim 13, wherein: The oxygen is derived from an oxygen-containing gas, and the reaction conditions of the air reactor are as follows: the reaction temperature is 600-1000℃, and the air space velocity is 1000-10000h -1 .

18. The method of claim 17, wherein: The reactor temperature of the air reactor is 600-1000 ℃.

19. The method of claim 1, wherein: The method comprises the following steps: (1) water vapor is subjected to magnetization treatment and then enters a steam reactor to react with a reduced oxygen carrier entering from the top of the steam reactor, so as to obtain hydrogen and an oxidized oxygen carrier; the hydrogen and unreacted water vapor flow out from the top of the steam reactor, and hydrogen is obtained after separation; (2) the oxidized oxygen carrier obtained in step (1) is subjected to deep oxidation reaction with oxygen in an air reactor; (3) the oxygen carrier after deep oxidation in step (2) is contacted with a reducing gas in a fuel reactor to obtain a reduced oxygen carrier, which is recycled to the steam reactor in step (1) to react with the water vapor subjected to magnetization treatment.

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