阅读说明：本技术 一种碳烃燃料等离子体催化链式制氢的方法 (Method for preparing hydrogen by catalyzing chain with carbon hydrocarbon fuel plasma ) 是由 吴芳芳 孔凡珺 朱珉 张潮海 谢声益 于 2021-01-18 设计创作，主要内容包括：本发明涉及一种碳烃燃料等离子体催化链式制氢的方法,包括滑动弧等离子体催化和链式制氢,滑动弧等离子体催化在滑动弧等离子体催化反应器中进行,滑动弧等离子体催化过程包括滑动弧等离子体重整和热催化重整两个阶段；链式制氢过程在链式制氢反应器中进行,采用Ni/Fe载氧体作为链式制氢过程氧载体；链式制氢过程包括Ni/Fe载氧体催化还原、制氢和氧化三阶段,完成碳烃燃料等离子体催化链式制氢。本发明的碳烃燃料等离子体链式制氢技术,两个反应器即可完成碳烃燃料催化重整制氢,缩短了碳烃燃料重整制氢的流程,实现了碳烃燃料重整制氢装备小型化和高效化,将链式制氢技术和滑动弧等离子体催化技术结合,实现高纯氢气制备和碳烃燃料重整废气CO-2的捕集。(The invention relates to a method for chain-type hydrogen production by plasma catalysis of a hydrocarbon fuel, which comprises sliding arc plasma catalysis and chain-type hydrogen production, wherein the sliding arc plasma catalysis is carried out in a sliding arc plasma catalytic reactor, and the sliding arc plasma catalysis process comprises two stages of sliding arc plasma reforming and thermocatalytic reforming; the chain type hydrogen production process is carried out in a chain type hydrogen production reactor, and a Ni/Fe oxygen carrier is used as an oxygen carrier in the chain type hydrogen production process; the chain type hydrogen production process comprises three stages of catalytic reduction of the Ni/Fe oxygen carrier, hydrogen production and oxidation, and the carbon hydrocarbon fuel plasma catalytic chain type hydrogen production is completed. According to the carbon hydrocarbon fuel plasma chained hydrogen production technology, the two reactors can complete the catalytic reforming hydrogen production of the carbon hydrocarbon fuel, the flow of the catalytic reforming hydrogen production of the carbon hydrocarbon fuel is shortened, the miniaturization and the high efficiency of the hydrogen production equipment of the carbon hydrocarbon fuel are realized, the chained hydrogen production technology and the sliding arc plasma catalysis technology are combined, the preparation of high-purity hydrogen and the CO (carbon monoxide) in the reforming exhaust gas of the carbon hydrocarbon fuel are realized 2 And (4) trapping.)

1. The carbon hydrocarbon fuel plasma catalysis chain type hydrogen production device is characterized by comprising a sliding arc plasma catalysis reactor (1) and a chain type hydrogen production reactor (2), wherein an outlet (1-4) of the sliding arc plasma catalysis reactor (1) is connected with an inlet (2-4) of the chain type hydrogen production reactor (2), and an outlet (2-5) of the chain type hydrogen production reactor (2) is connected with an inlet (3-1) of a condenser (3).

2. The carbon hydrocarbon fuel plasma catalytic chain type hydrogen production device according to claim 1, characterized in that: the sliding arc plasma catalytic reactor (1) comprises a sliding arc plasma reforming module (1-1) and a thermal catalytic reforming module (1-2); the sliding arc plasma reforming module (1-1) is communicated with a gas inlet (1-3) of the sliding arc plasma catalytic reactor (1), and the chain type hydrogen production reactor (2) comprises a Ni/Fe oxygen carrier catalytic reduction module (2-1), a hydrogen production (2-2) module and an oxidation module (2-3).

3. A carbon hydrocarbon fuel plasma catalysis chain type hydrogen production method is characterized in that: the method comprises the following steps:

s1: sliding arc plasma catalysis: the method is carried out in a sliding arc plasma catalytic reactor (1), and the sliding arc plasma catalytic process comprises two stages of sliding arc plasma reforming and thermocatalytic reforming;

s2: chain hydrogen production: the chain hydrogen production process is carried out in a chain hydrogen production reactor (2), and a Ni/Fe oxygen carrier is used as an oxygen carrier in the chain hydrogen production process; the chain type hydrogen production process comprises three stages of catalytic reduction of Ni/Fe oxygen carrier, hydrogen production and oxidation;

and completing the carbon hydrocarbon fuel plasma catalysis chain type hydrogen production.

4. The carbon hydrocarbon fuel plasma catalytic chain hydrogen production method according to claim 3, wherein the step S1 specifically comprises: the carbon hydrocarbon fuel and the oxidizing gas (a) enter from a gas inlet (1-3) of the sliding arc plasma catalytic reactor (1); in the sliding arc plasma reforming stage (1-1), the hydrocarbon fuel and the steam are heated by the discharge plasma, and the hydrocarbon fuel and the steam are converted into small molecular hydrocarbons; the unreacted carbon hydrocarbon fuel and the oxidizing gas enter a thermal catalytic reforming stage to generate a thermal catalytic reforming reaction, and the carbon hydrocarbon fuel and the steam are completely converted into CO and H due to the fact that the thermal catalytic reforming is a strong endothermic reaction₂And a small molecule hydrocarbon (b).

5. The carbon hydrocarbon fuel plasma catalytic chain hydrogen production method according to claim 4, characterized in that: in the step S1, the oxidizing gas at the gas inlet (a) of the sliding arc plasma catalytic reactor (1) contains water vapor and O₂And CO₂。

6. The carbon hydrocarbon fuel plasma catalytic chain hydrogen production method according to claim 4, characterized in that: in the step S1, the sliding arc plasma catalytic reactor (1) adopts the catalyst active components of Ni, Pt and Cu for the thermocatalytic reforming (1-2); the catalyst carrier is Al₂O₃、MgAl₂O₃、ZrO₂And TiO₂。

7. The carbon hydrocarbon fuel plasma catalytic chain type hydrogen production device according to claim 4, characterized in that: the sliding arc plasma catalytic reactor (1) is operated intermittently and is opened only in the catalytic reduction stage (2-1) of the chain type hydrogen production reactor (2), and the sliding arc plasma catalytic reactor (1) provides reducing gases CO and H for the catalytic reduction stage (2-1) of the chain type hydrogen production reactor (2)₂And a small molecule hydrocarbon (b).

8. The carbon hydrocarbon fuel plasma catalytic chain type hydrogen production device according to claim 4, characterized in that: the step S1: the carbon hydrocarbon fuel and the water vapor are heated to 800-1000 ℃ by the discharge plasma, and the conversion rate of the carbon hydrocarbon fuel is 40-50%; CO, H₂And the gas temperature of the small molecular hydrocarbon (b) is reduced to 600-700 ℃.

9. The carbon hydrocarbon fuel plasma catalytic chain hydrogen production method according to claim 3, wherein the step S2 specifically comprises: in the catalytic reduction stage, the Ni/Fe oxygen carrier metal oxide and CO and H entering from the inlet (2-4) of the chain type hydrogen production reactor (2)₂Reacting with small molecule hydrocarbon (b) to generate gas product CO₂And steam (c), the Ni/Fe oxygen carrier is reduced to elemental Ni and Fe/FeO, CO₂And the water vapor (c) is condensed by the condenser (3) to obtain pure CO₂(h) (ii) a In the hydrogen production stage, steam (d) is introduced into an inlet (2-4) of the chain hydrogen production reactor (2), and Fe/FeO reacts with the steam (d) to generate Fe₃O₄The gaseous product comprises H₂And water vapor (e), H₂And the water vapor (e) is condensed by the condenser (3) to obtain pure H₂(i) (ii) a In the oxidation stage, air (f) and Fe are introduced into an inlet (2-4) of the chain type hydrogen production reactor (2)₃O₄And Ni is sufficiently oxidized by oxidation in air (f) to realize regeneration of oxygen carrier。

Technical Field

The invention relates to the field of hydrogen production by reforming, in particular to a method for producing hydrogen by catalyzing chain type carbon hydrocarbon fuel plasma.

Background

Hydrogen is not only an important chemical fuel, but also a clean fuel, and plays an increasingly important role in modern industries, fuel cells and other industries. With the increasing demand for clean fuels, higher requirements are put on hydrogen production devices. The traditional process for preparing pure hydrogen by reforming hydrocarbon fuel is complex and needs to undergo the processes of catalytic reforming, high-temperature water gas shift, low-temperature water gas shift, CO preferential oxidation and pressure swing adsorption. Catalytic reforming and pressure swing adsorption are high energy consumption processes, a hydrocarbon fuel combustion reactor is required to provide heat for catalytic reforming, and pressure swing adsorption is required to be completed under high pressure and a compressor and a high-pressure cavity are required to be arranged.

The sliding arc plasma catalysis technology is a new technology applying plasma, and has the advantages that: the method has the advantages of quick start, high thermal efficiency and moderate reaction temperature, but when the technology is used for reforming hydrocarbon fuel, the efficiency of converting diesel oil C, H into CO can only reach 80 percent at most, and the gas product contains a large amount of small molecular hydrocarbon. The chain hydrogen production technology is a common hydrogen production technology and has the advantages that: high purity of hydrogen production and complete conversion of fuel gas into H₂O and CO₂Only condensation is needed to realize CO₂And (4) trapping. However, when the chain hydrogen production technology is used for treating macromolecular hydrocarbons, the problems of coking and carbon deposition are easy to occur, and the hydrogen production efficiency is influenced.

Disclosure of Invention

In order to solve the technical problem, the invention provides a method for producing hydrogen by plasma catalysis chain of carbon hydrocarbon fuel.

The technical scheme adopted by the invention is as follows:

a chain type hydrogen production device for catalyzing carbon hydrocarbon fuel plasma comprises a sliding arc plasma catalytic reactor and a chain type hydrogen production reactor, wherein an outlet of the sliding arc plasma catalytic reactor is connected with an inlet of the chain type hydrogen production reactor, and an outlet of the chain type hydrogen production reactor is connected with an inlet of a condenser.

Preferably, the sliding arc plasma catalytic reactor comprises a sliding arc plasma reforming module and a thermal catalytic reforming module; the sliding arc plasma reforming module is communicated with a gas inlet of the sliding arc plasma catalytic reactor, and the chain type hydrogen production reactor comprises a Ni/Fe oxygen carrier catalytic reduction module, a hydrogen production module and an oxidation module.

A carbon hydrocarbon fuel plasma catalyzed chained hydrogen production method, comprising the steps of:

s1: sliding arc plasma catalysis: the method is carried out in a sliding arc plasma catalytic reactor, and the sliding arc plasma catalytic process comprises two stages of sliding arc plasma reforming and thermocatalytic reforming;

s2: chain hydrogen production: the chain type hydrogen production process is carried out in a chain type hydrogen production reactor, and a Ni/Fe oxygen carrier is used as an oxygen carrier in the chain type hydrogen production process; the chain type hydrogen production process comprises three stages of catalytic reduction of Ni/Fe oxygen carrier, hydrogen production and oxidation;

and completing the carbon hydrocarbon fuel plasma catalysis chain type hydrogen production.

Preferably, the step S1 specifically includes: a hydrocarbon fuel and an oxidizing gas (a) are introduced from a sliding arc plasma catalytic reactor gas inlet; in the sliding arc plasma reforming stage, the hydrocarbon fuel and the steam are heated by the discharge plasma, and the hydrocarbon fuel and the steam are converted into small molecular hydrocarbons; the unreacted carbon hydrocarbon fuel and the oxidizing gas enter a thermal catalytic reforming stage to generate a thermal catalytic reforming reaction, and the carbon hydrocarbon fuel and the steam are completely converted into CO and H due to the fact that the thermal catalytic reforming is a strong endothermic reaction₂And a small molecule hydrocarbon (b).

Further preferably, in the step S1, the sliding arc plasma catalytic reactor gas inlet (a) contains water vapor, O₂And CO₂。

Further preferably, in the step S1, the sliding arc plasma catalytic reactor thermal catalytic reforming (1-2) adopts catalytic active components of metals Ni, Pt and Cu; catalytic converterThe agent carrier is Al₂O₃、MgAl₂O₃、ZrO₂And TiO₂。

Further preferably, the sliding arc plasma catalytic reactor is operated intermittently and is opened only in the catalytic reduction stage of the chain type hydrogen production reactor, and the sliding arc plasma catalytic reactor provides reducing gases of CO and H for the catalytic reduction stage of the chain type hydrogen production reactor₂And a small molecule hydrocarbon (b).

Further preferably, the step S1: the carbon hydrocarbon fuel and the water vapor are heated to 800-1000 ℃ by the discharge plasma, and the conversion rate of the carbon hydrocarbon fuel is 40-50%; CO, H₂And the gas temperature of the small molecular hydrocarbon (b) is reduced to 600-700 ℃.

Preferably, the step S2 specifically includes: in the catalytic reduction stage, the Ni/Fe oxygen carrier metal oxide and CO and H entering from the inlet of the chain type hydrogen production reactor₂Reacting with small molecule hydrocarbon (b) to generate gas product CO₂And steam (c), the Ni/Fe oxygen carrier is reduced to elemental Ni and Fe/FeO, CO₂And water vapor (c) is condensed by the condenser and pure CO is obtained₂(h) (ii) a In the hydrogen production stage, steam (d) is introduced into the inlet of the chain hydrogen production reactor, and Fe/FeO reacts with the steam (d) to generate Fe₃O₄The gaseous product comprises H₂And water vapor (e), H₂And water vapor (e) is condensed by the condenser and pure H is obtained₂(i) (ii) a In the oxidation stage, air (f) and Fe are introduced into the inlet of the chain type hydrogen production reactor₃O₄And Ni is sufficiently oxidized by oxidation in air (f) to realize oxygen carrier regeneration.

The invention has the following effects: the carbon hydrocarbon fuel plasma chained hydrogen production technology has a simple structure, can complete the catalytic reforming hydrogen production of the carbon hydrocarbon fuel by carrying out two reactors, shortens the hydrogen production flow of the carbon hydrocarbon fuel reforming, and realizes the miniaturization and high efficiency of the carbon hydrocarbon fuel reforming hydrogen production equipment;

(2) the invention combines the chain hydrogen production technology and the sliding arc plasma catalysis technology to obtainHigh conversion efficiency of hydrocarbon fuel, high purity hydrogen preparation and CO in hydrocarbon fuel reforming exhaust gas₂Trapping;

(3) the sliding arc plasma discharge device has compact structure and large gas treatment capacity, is a sliding arc plasma discharge device with the height of 20 cm, has the carbon hydrocarbon fuel treatment capacity of 0.3L/min, and is suitable for quickly reforming the carbon hydrocarbon fuel to prepare hydrogen. In contrast, the gas throughput per minute of a conventional micro carbon hydrocarbon fuel reforming reactor is only on the order of milliliters. The sliding arc plasma is a typical warm plasma, the actual temperature of the plasma can reach 800-1000 ℃, the gas temperature of the hydrocarbon fuel passes through the sliding arc reactor, and the gas temperature is rapidly increased to 800-1000 ℃ to provide heat for the subsequent catalytic reforming of the hydrocarbon fuel.

Drawings

FIG. 1 is a block diagram of the overall structure of a carbon hydrocarbon fuel plasma catalytic chain hydrogen production device provided by the invention;

wherein: the system comprises a sliding arc plasma catalytic reactor 1, a sliding arc plasma reforming module 1-1, a thermal catalytic reforming module 1-2, a gas inlet 1-3 of the sliding arc plasma catalytic reactor, an outlet 1-4 of the sliding arc plasma catalytic reactor, a chain type hydrogen production reactor 2, an inlet 2-4 of the chain type hydrogen production reactor, an outlet 2-5 of the chain type hydrogen production reactor, an Ni/Fe oxygen carrier catalytic reduction module 2-1, a hydrogen production module 2-2, an oxidation module 2-3, a condenser 3 and an inlet 3-1 of the condenser;

fig. 2 is a schematic diagram of an embodiment of a carbon hydrocarbon fuel plasma chain hydrogen production device provided by the invention.

Detailed Description

The present invention will be described in further detail with reference to specific examples, but the embodiments of the present invention are not limited to the scope of the examples. These examples are intended to illustrate the invention only and are not intended to limit the scope of the invention.

Example 1

A chain type hydrogen production device for catalyzing carbon hydrocarbon fuel plasma comprises a sliding arc plasma catalytic reactor 1 and a chain type hydrogen production reactor 2, wherein an outlet 1-4 of the sliding arc plasma catalytic reactor 1 is connected with an inlet 2-4 of the chain type hydrogen production reactor 2, and an outlet 2-5 of the chain type hydrogen production reactor 2 is connected with an inlet 3-1 of a condenser 3.

Preferably, the sliding arc plasma catalytic reactor 1 comprises a sliding arc plasma reforming module 1-1 and a thermal catalytic reforming module 1-2; the sliding arc plasma reforming module 1-1 is communicated with a gas inlet 1-3 of the sliding arc plasma catalytic reactor 1, and the chain type hydrogen production reactor 2 comprises a Ni/Fe oxygen carrier catalytic reduction module 2-1, a hydrogen production 2-2 module and an oxidation module 2-3.

A carbon hydrocarbon fuel plasma catalyzed chained hydrogen production method, comprising the steps of:

s1: sliding arc plasma catalysis: the method is carried out in a sliding arc plasma catalytic reactor 1, and the sliding arc plasma catalytic process comprises two stages of sliding arc plasma reforming and thermocatalytic reforming;

s2: chain hydrogen production: the chain hydrogen production process is carried out in the chain hydrogen production reactor 2, and a Ni/Fe oxygen carrier is used as an oxygen carrier in the chain hydrogen production process; the chain type hydrogen production process comprises three stages of catalytic reduction of Ni/Fe oxygen carrier, hydrogen production and oxidation;

and completing the carbon hydrocarbon fuel plasma catalysis chain type hydrogen production.

Preferably, the step S1 specifically includes: the hydrocarbon fuel and the oxidizing gas (a) enter from gas inlets 1-3 of the sliding arc plasma catalytic reactor 1; in the sliding arc plasma reforming stage 1-1, the hydrocarbon fuel and the steam are heated by the discharge plasma, and the hydrocarbon fuel and the steam are converted into small molecular hydrocarbons; the unreacted carbon hydrocarbon fuel and the oxidizing gas enter a thermal catalytic reforming stage to generate a thermal catalytic reforming reaction, and the carbon hydrocarbon fuel and the steam are completely converted into CO and H due to the fact that the thermal catalytic reforming is a strong endothermic reaction₂And a small molecule hydrocarbon (b).

Further preferably, in the step S1, the oxidizing gas at the gas inlet (a) of the sliding arc plasma catalytic reactor 1 contains water vapor and O₂And CO₂。

Further preferably, in the step S1, the sliding arc plasma catalytic reactor 1 adopts the thermal catalytic reforming 1-2The active components of the catalyst are metal Ni, Pt and Cu; the catalyst carrier is Al₂O₃、MgAl₂O₃、ZrO₂And TiO₂。

Further preferably, the sliding arc plasma catalytic reactor 1 is intermittently operated and is only opened during the catalytic reduction stage 2-1 of the chain type hydrogen production reactor 2, and the sliding arc plasma catalytic reactor 1 supplies reducing gases CO and H to the catalytic reduction stage 2-1 of the chain type hydrogen production reactor 2₂And a small molecule hydrocarbon (b).

Further preferably, the step S1: the carbon hydrocarbon fuel and the water vapor are heated to 800-1000 ℃ by the discharge plasma, and the conversion rate of the carbon hydrocarbon fuel is 40-50%; CO, H₂And the gas temperature of the small molecular hydrocarbon (b) is reduced to 600-700 ℃.

Further preferably, the step S2 specifically includes: in the catalytic reduction stage, the Ni/Fe oxygen carrier metal oxide and CO and H entering from the inlet 2-4 of the chain type hydrogen production reactor 2₂Reacting with small molecule hydrocarbon (b) to generate gas product CO₂And steam (c), the Ni/Fe oxygen carrier is reduced to elemental Ni and Fe/FeO, CO₂And water vapor (c) is passed through a condenser 3 to condense the water vapor and obtain pure CO₂(h) (ii) a In the hydrogen production stage, steam (d) is introduced into an inlet 2-4 of the chain type hydrogen production reactor 2, and Fe/FeO reacts with the steam (d) to generate Fe₃O₄The gaseous product comprises H₂And water vapor (e), H₂And water vapor (e) is condensed by the condenser 3 to obtain pure H₂(i) (ii) a In the oxidation stage, air (f) and Fe are introduced into an inlet 2-4 of the chain type hydrogen production reactor 2₃O₄And Ni is sufficiently oxidized by oxidation in air (f) to realize oxygen carrier regeneration.

Example 1

As shown in fig. 1, the sliding arc plasma catalytic process is performed in a sliding arc plasma catalytic reactor 1, and the sliding arc plasma catalytic process includes two stages, namely sliding arc plasma reforming 1-1 and thermal catalytic reforming 1-2; sliding arc plasma catalytic reactor 1 for hydrocarbon fuel and oxidizing gas aGas inlet 1-3, oxidizing gas (a) containing water vapor, O₂And CO₂(ii) a In a sliding arc plasma reforming stage 1-1, the carbon hydrocarbon fuel and the steam are heated to 800-1000 ℃ by the discharge plasma, the carbon hydrocarbon fuel and the steam are converted into micromolecular hydrocarbon, the conversion rate of the carbon hydrocarbon fuel is 40-50%, and the chemical reaction in the stage is shown as follows; unreacted carbon hydrocarbon fuel and oxidizing gas enter a thermal catalytic reforming stage 1-2 to generate a thermal catalytic reforming reaction, and the carbon hydrocarbon fuel and water vapor are completely converted into CO and H due to the fact that the thermal catalytic reforming is a strong endothermic reaction₂And a small molecular hydrocarbon (b), wherein the gas temperature is reduced to 600-700 ℃, and the active components of the catalyst adopted in the stage are metal Ni, metal Pt and metal Cu; the catalyst carrier is Al₂O₃、MgAl₂O₃、ZrO₂And TiO.

As shown in figure 1, the chain hydrogen production process is carried out in a chain hydrogen production reactor (2), and a Ni/Fe oxygen carrier is used as an oxygen carrier in the chain hydrogen production process; the chain type hydrogen production process comprises three stages of catalytic reduction 2-1 of Ni/Fe oxygen carrier, hydrogen production 2-2 and oxidation 2-3; in the catalytic reduction stage, the Ni/Fe oxygen carrier metal oxide and CO and H entering from the inlet 2-4 of the chain type hydrogen production reactor 2₂Reacting with small molecule hydrocarbon (b) to generate gas product CO₂And steam (c), the Ni/Fe oxygen carrier is reduced to elemental Ni and Fe/FeO, CO₂And water vapor (c) is passed through a condenser 3 to condense the water vapor and obtain pure CO₂(h) The reaction temperature at this stage is 800-1000 ℃; in the hydrogen production stage, steam (d) is introduced into an inlet 2-4 of the chain type hydrogen production reactor 2, and Fe/FeO reacts with the steam (d) to generate Fe₃O₄The gaseous product comprises H₂And water vapor (e), H₂And water vapor (e) is condensed by the condenser 3 to obtain pure H₂(i) The reaction temperature at this stage was 700 ℃; in the oxidation stage, air (f) and Fe are introduced into an inlet 2-4 of the chain type hydrogen production reactor 2₃O₄And Ni is fully oxidized by oxidation in air (f) to realize oxygen carrier regeneration, and the reaction temperature at the stage is 900-1000 ℃; n in 2 Ni/Fe oxygen carrier of chain type hydrogen production reactorThe i oxide is a catalytic active component, and the Fe oxide has the functions of oxygen release and hydrogen production.

Example 3

FIG. 2 shows a schematic diagram of a carbon hydrocarbon fuel plasma chained hydrogen production device, which is suitable for the demand of submarine deep sea hydrogen production. High carbon hydrocarbon fuel oil is filled in the fuel tank, passes through the gas circuit module and comes from O of the cathode outlet of the fuel cell₂And water vapor are heated to 200 ℃ and mixed to enter the sliding arc plasma catalytic reactor. In the sliding arc plasma catalytic reactor, the mixed gas is heated to 800-1000 ℃ by discharge plasma and undergoes thermocatalytic reforming reaction, and high-carbon hydrocarbon fuel oil, water vapor and oxygen are completely converted into CO and H due to the thermocatalytic reforming reaction which is a strong endothermic reaction₂And small molecular hydrocarbon, and the sliding arc plasma catalytic reactor adopts Ni/Al as catalyst₂O₃。

In the chain hydrogen production process, a Ni/Fe oxygen carrier is used as an oxygen carrier in the chain hydrogen production reactor; the chain type hydrogen production process comprises three stages of catalytic reduction of Ni/Fe oxygen carrier, hydrogen production and oxidation; in the catalytic reduction stage, the sliding arc plasma catalytic reactor is driven by a high-voltage direct-current power supply, and products CO and H₂And micromolecular hydrocarbon enters through the gas circuit module and reacts with the Ni/Fe oxygen carrier metal oxide in a reduction way to generate a gas product CO₂And steam, the Ni/Fe oxygen carrier is reduced to elemental Ni and Fe/FeO, CO₂And the water vapor is condensed in the gas circuit module, and pure CO is obtained₂Outlet of condenser CO₂And steam temperature of 70 ℃ CO₂Into CO₂A storage tank which is compressed and discharged into deep sea; because the chain reactor is connected with the sliding arc plasma catalytic reactor, the heat of the sliding arc catalytic reactor maintains the reaction temperature of 800-; in the hydrogen production stage, water vapor from the cathode outlet of the fuel cell enters the chain type hydrogen production reactor through the gas circuit module, and Fe/FeO reacts with the water vapor to generate Fe₃O₄The gaseous product is H₂，H₂Introducing into a hydrogen storage tank for power generation of the fuel cell, wherein the reaction temperature at the stage is 700 ℃; in the oxidation stage, the inlet of the chain type hydrogen production reactor is communicatedOxygen, Fe, from the cathode outlet of the fuel cell₃O₄And Ni is fully oxidized by oxygen to realize the regeneration of the oxygen carrier, and the reaction temperature at the stage is 900-1000 ℃; ni oxide in the Ni/Fe oxygen carrier of the chain type hydrogen production reactor is a catalytic active component, and Fe oxide plays a role in oxygen release and hydrogen production.

The device has compact structure, height of 50 cm, length of 40 cm and width of 40 cm. The reactor adopts a modular design, the core component is a plasma catalytic reactor, the plasma catalytic reactor is driven by a high-voltage direct-current power supply, the voltage is 10 kV, the size of the reactor is compact, the height is 30 cm, the width is 20 cm, and the depth is 20 cm. The consumption speed of the hydrocarbon fuel is 0.3L/min, the generation speed of the hydrogen is 6L/min, and the purity of the hydrogen is over 99.9 percent. The hydrogen produced by the device is directly introduced into a hydrogen storage tank for fuel cells, and the CO is collected₂Introducing CO via a compressor₂After the high-pressure storage tank is used, the submarine can be directly discharged into the sea when being navigated in deep sea.