A device and method for preparing hydrogen from biomass chemical chain carbonization catalytic materials

Abstract

The present invention relates to the technical fields of functional materials, energy conversion and environmental protection, and in particular to a device and method for preparing hydrogen from biomass chemical chain carbonization catalytic materials. An air distribution plate is provided in the reactor, which divides the reactor cavity into an upper biomass chemical chain carbonization reactor and a lower catalyst regeneration combustion chamber; the biomass chemical chain carbonization reactor utilizes MO x Lattice oxygen realizes biomass carbonization, while MO x The catalyst regeneration combustion chamber is used to reduce the M particles and evenly load them on the surface of biochar to form M / C catalyst. The high-temperature gas with heat generated by the combustion in the catalyst regeneration combustion chamber enters the biomass chemical chain carbonization reactor upward through the air distribution plate, providing heat energy for the biomass carbonization reaction. The catalyst regeneration combustion chamber is also used to activate the spent M / C catalyst into MO. x The method of the present invention realizes CO2 gas capture and energy cascade utilization, and effectively solves the problem of easy deactivation of methanol steam reforming hydrogen production catalyst.

Description

Technical Field

[0001] The present invention relates to the technical fields of functional materials, energy conversion and environmental protection, and in particular to a device and method for preparing biomass chemical chain carbonization catalytic materials and co-producing hydrogen. Background Art

[0002] As a hydrogen carrier, methanol has significant advantages in hydrogen production, which are reflected in its wide source, low price, no need to activate CC bonds, low conversion temperature, high hydrogen-carbon molar ratio, and 2.1L of hydrogen can be produced per unit mass of methanol. By inputting methanol into the vehicle, methanol is catalytically converted in situ in the on-board reactor to produce hydrogen for fuel cell power generation, which can indirectly solve the problem of hydrogen storage and transportation. However, the sintering and deactivation of the catalyst will lead to a decrease in hydrogen production, or even the inability to produce hydrogen. The catalyst activation process requires very high temperatures and reducing gases, such as hydrogen, which will consume energy and increase costs.

[0003] Catalyst activation can be achieved through the biomass carbonization process. Biomass is widely distributed, renewable, and low-pollution. Biomass carbonization technology optimizes and utilizes biomass energy, significantly saving coal and forest resources. The biochar and syngas produced can also be used to reduce and activate catalysts. However, current biomass carbonization technology utilizes a fixed bed, requiring significant heat and air for the carbonization reaction. This process is uncontrollable and produces significant amounts of pollutants and CO2 gas. Reducing CO2 emissions and energy consumption are key challenges in the biomass carbonization process. Summary of the Invention

[0004] In order to solve the current problem of deactivation of methanol hydrogen production catalysts and at the same time achieve energy conservation and emission reduction during the catalyst activation process, the first purpose of the present invention is to propose a method for preparing and co-producing hydrogen by biomass chemical chain carbonization catalytic materials that integrates chemical chain conversion and biomass carbonization. At the same time, a reaction device matching this method is correspondingly proposed, aiming to achieve biomass chemical chain carbonization and methanol hydrogen production catalyst activation through the device.

[0005] The second purpose of the present invention is to provide a new reactor device for realizing chemical chain biomass carbonization and catalyst activation, which is a moving bed reactor separated by air distribution plates. The purpose is to use the innovative reactor to regulate the components of the reducing product, and utilize the products and waste heat to realize catalyst regeneration and step-by-step energy utilization.

[0006] The third purpose of the present invention is to provide a new reactor device for realizing biomass chemical chain carbonization and catalyst preparation and regeneration, which is a moving bed reactor separated by air distribution plates. The purpose is to use the innovative reactor to provide a mobile carrier with a methanol steam reforming hydrogen production catalyst with biochar-supported active component M.

[0007] The fourth purpose of the present invention is to provide a new reactor device for realizing biomass chemical chain carbonization and catalyst preparation and regeneration, which is a moving bed reactor separated by air distribution plates. The purpose is to use the new reactor to burn C in the deactivated M / C catalyst to provide heat and realize the regeneration of active components.

[0008] The fifth object of the present invention is to propose a method for preparing hydrogen by carbonizing biomass chemical chain catalytic materials in accordance with the first object. x -M-MO x The biomass is oxidized by lattice oxygen. Correspondingly, O2 is used to activate and regenerate the catalyst.

[0009] In the present invention, the oxygen carrier provides lattice oxygen during the biomass chemical chain carbonization process to realize the biomass carbonization reaction. The biomass carbonization product can be selectively controlled by regulating the carbon / biomass ratio. At the same time, the oxygen carrier is reduced and mixed with biochar to form an M / C catalyst, which can realize the catalytic methanol in-situ hydrogen production driving vehicle; the deactivated catalyst M / C is collected in the moving bed combustion chamber, wherein C participates in combustion and M is oxidized and regenerated. This process realizes the preparation and regeneration of the methanol hydrogen production catalyst.

[0010] Specific technical solutions:

[0011] A biomass chemical chain carbonization catalytic material preparation and co-production of hydrogen device, comprising a reactor, wherein an air distribution plate is provided in the reactor, and the air distribution plate divides the reactor cavity into an upper biomass chemical chain carbonization reactor and a lower catalyst regeneration combustion chamber;

[0012] Biomass chemical chain carbonization reactor using MO x Lattice oxygen realizes biomass carbonization, while MO x Reduction, and the generated M particles are uniformly supported on the surface of biochar to form M / C catalyst;

[0013] The high-temperature gas with heat generated by the combustion in the catalyst regeneration combustion chamber enters the biomass chemical chain carbonization reactor upward through the air distribution plate, providing heat energy for the biomass carbonization reaction; the catalyst regeneration combustion chamber is also used to activate the spent M / C catalyst into MO x ;

[0014] The top feed port of the biomass chemical chain carbonization reactor is connected to a screw feeder for biomass to enter;

[0015] The bottom discharge port of the biomass chemical chain carbonization reactor is connected to the feed port of the methanol reforming chamber through the first U-valve turner, providing the methanol reforming chamber with fresh M / C catalyst for methanol hydrogen production;

[0016] The discharge port of the methanol reforming chamber is connected to the feed port of the catalyst regeneration combustion chamber; the spent M / C catalyst in the methanol reforming chamber enters the catalyst regeneration combustion chamber;

[0017] The outlet of the catalyst regeneration combustion chamber is connected to the circulation inlet at the top of the biomass chemical chain carbonization reactor through the second U-valve turner, and the MO x Sent into the biomass chemical chain carbonization reactor;

[0018] The exhaust port at the top of the biomass chemical chain carbonization reactor is connected to the feed port of the catalyst regeneration combustion chamber through an air inlet system, supplying the synthesis gas generated by the biomass chemical chain carbonization into the catalyst regeneration combustion chamber; the feed port of the catalyst regeneration combustion chamber is also supplied with oxygen through the air inlet system.

[0019] The air intake system comprises an air pump, a pressure reducing valve and a flow meter which are connected in sequence.

[0020] A method for preparing co-production of hydrogen by biomass chemical chaining carbonization catalytic material, using a device for preparing co-production of hydrogen by biomass chemical chaining carbonization catalytic material, the method comprising the following steps:

[0021] The biomass is fed into the biomass chemical chain carbonization reactor using a screw feeder and mixed with MO x At the same time, they fall in and react at high temperature to generate biosynthesis gas, while the biomass is carbonized to generate biochar;

[0022] MO in biomass chemical chaining carbonization reactor x The catalyst is reduced to M particles and highly dispersed on the biochar material to form a fresh M / C catalyst. The fresh M / C catalyst enters the methanol reforming chamber through the first U-valve tipper and generates H2 and CO2 under catalytic and reaction conditions for fuel cell power generation.

[0023] The deactivated M / C catalyst is recycled to the catalyst regeneration combustion chamber, and under the conditions of O2 and high temperature, the M of the M / C catalyst undergoes surface exchange with O2, and the oxygen ions are further transferred to the M lattice to form a stable MO x , to activate the catalytic active components, C burns to generate heat; then it is fed into the biomass chemical chain carbonization reactor through the second U-valve turner;

[0024] The synthesis gas flow generated in the biomass chemical chain carbonization reactor is partially recycled to the bottom catalyst regeneration combustion chamber to achieve energy cascade utilization.

[0025] The biomass carbonization reaction temperature in the biomass chemical chain carbonization reactor is 200-350°C.

[0026] The reaction temperature of the catalyst regeneration combustion chamber is 350-450°C.

[0027] The methanol steam reforming reaction temperature in the methanol reforming chamber is in the range of 200 to 300°C, preferably 200 to 240°C.

[0028] The MO x and an M / C catalyst, wherein M is Cu, Pd, Ru or Rh;

[0029] The composition of the synthesis gas can be adjusted according to the different biomass ratios. When the biomass ratio is high, the composition is CO2 and H2O; when the biomass ratio is low, the composition is CO2, CO, H2O, CH4 and other synthesis gases.

[0030] The methanol reforming chamber is a tubular reactor.

[0031] The catalyst regeneration combustion chamber is a bubbling bed reactor;

[0032] The biomass chemical chain carbonization reactor type is a moving bed reactor.

[0033] Compared with the prior art, the present invention has the following advantages:

[0034] 1) The method of the present invention provides the oxygen required for biomass carbonization through the release of (M=Cu / Ru / Rh / Pd) lattice oxygen, achieving flameless carbonization of biomass to produce biochar and adjustable product gas. Synthesis gas or CO2 and H2O are generated by adjusting the ratio of Cu / Biomass, avoiding N and S oxide pollution. At the same time, CO2 gas is captured and recovered to provide heat, thereby achieving CO2 gas capture;

[0035] 2) This device recovers the high-temperature reaction products CO2 and H2O or synthesis gas and introduces them into the regenerative combustion chamber. The synthesis gas can be used for combustion to provide the reaction heat required for the carbonization of the biomass chemical chain. The heat carried by the high-temperature CO2 and H2O itself can improve the utilization of waste heat and realize the cascade utilization of energy.

[0036] 3) The device and method of the present invention can simultaneously produce a green and recyclable methanol steam reforming catalytic material while achieving biomass chemical chain carbonization. During the biomass chemical chain carbonization reaction, the released oxygen is reduced to M metal, and the biomass is carbonized to produce biochar. The M metal is evenly dispersed on the biochar carrier to produce M / C catalytic material for catalytic hydrogen production in a mobile hydrogen production reactor. After deactivation, it is recycled to the regeneration combustion chamber for oxidation and activation, effectively solving the problem of easy deactivation of methanol steam reforming hydrogen production catalysts.

[0037] 4) The device of the present invention provides a reactor, and the biomass chemical chain carbonization reactor and the regeneration combustion chamber are separated by an air distribution plate. The solid material is transported from the biomass chemical chain carbonization reactor to the mobile hydrogen production reactor through a U-valve turner, and the deactivated catalyst enters the regeneration combustion chamber for activation. The CO2 and H2O produced by combustion can enter the upper biomass chemical chain carbonization reactor through the air distribution plate to provide heat. This device saves material collection and transportation costs, realizes self-heating, and improves energy utilization efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 Schematic diagram of the device structure of the present invention;

[0039] Figure 2 Schematic diagram of the method principle of the present invention;

[0040] Figure 3 Schematic diagram of the chemical chain cycle process of the present invention;

[0041] Figure 4 This is a graph showing the concentration of gas products from biomass chemical chain carbonization in an embodiment;

[0042] Figure 5 This is a graph showing the conversion rate of Cu / C-catalyzed methanol steam reforming in Example 1;

[0043] Figure 6 This is a graph showing the hydrogen atom utilization efficiency of Cu / C-catalyzed methanol steam reforming in Example 2;

[0044] Figure 7 This is the product selectivity diagram of Cu / C catalyzed methanol steam reforming in Example 1. DETAILED DESCRIPTION

[0045] The present invention will be further described below with reference to the embodiments and accompanying drawings.

[0046] like Figure 1 As shown, a biomass chemical chain carbonization catalytic material preparation and co-production of hydrogen device includes a reactor 7, wherein an air distribution plate 5 is provided in the reactor 7, and the air distribution plate 5 divides the inner cavity of the reactor 7 into an upper biomass chemical chain carbonization reactor 9 and a lower catalyst regeneration combustion chamber 8;

[0047] Biomass chemical chain carbonization reactor 9 uses MO x Lattice oxygen realizes biomass carbonization, while MO x Reduction, and the generated M particles are uniformly supported on the surface of biochar to form M / C catalyst;

[0048] The high-temperature gas with heat generated by the combustion in the catalyst regeneration combustion chamber 8 enters the biomass chemical chain carbonization reactor 9 upward through the air distribution plate 5, providing heat energy for the biomass carbonization reaction; the catalyst regeneration combustion chamber 8 is also used to activate the spent M / C catalyst into MO x ;

[0049] The top feed port of the biomass chemical chain carbonization reactor 9 is connected to a screw feeder 6 for the biomass to enter;

[0050] The bottom discharge port of the biomass chemical chain carbonization reactor 9 is connected to the feed port of the methanol reforming chamber 10 through the first U-valve turner 4, providing the methanol reforming chamber 10 with fresh M / C catalyst for methanol hydrogen production;

[0051] The discharge port of the methanol reforming chamber 10 is connected to the feed port of the catalyst regeneration combustion chamber 8; the spent M / C catalyst in the methanol reforming chamber 10 enters the catalyst regeneration combustion chamber 8;

[0052] The discharge port of the catalyst regeneration combustion chamber 8 is connected to the circulation inlet at the top of the biomass chemical chain carbonization reactor 9 through the second U-valve turner 11, and the MO x Sent into the biomass chemical chain carbonization reactor 9;

[0053] The top exhaust port of the biomass chemical chain carbonization reactor 9 is connected to the feed port of the catalyst regeneration combustion chamber 8 through an air inlet system, supplying the synthesis gas generated by the biomass chemical chain carbonization to the catalyst regeneration combustion chamber 8; the feed port of the catalyst regeneration combustion chamber 8 is also supplied with oxygen through the air inlet system.

[0054] The air intake system includes an air pump 1, a pressure reducing valve 2 and a flow meter 3 which are connected in sequence.

[0055] like Figure 2 As shown, a method for preparing co-production of hydrogen by biomass chemical chaining carbonization catalytic material, using the above-mentioned biomass chemical chaining carbonization catalytic material to prepare co-production of hydrogen device, the method comprising the following steps:

[0056] The biomass is fed into the biomass chemical chain carbonization reactor 9 by a screw feeder 6 and mixed with the MO x At the same time, they fall in and react at high temperature to generate biosynthesis gas, while the biomass is carbonized to generate biochar;

[0057] Biomass chemical chain carbonization reactor 9 MO x The catalyst is reduced to M particles and highly dispersed on the biochar material to form a fresh M / C catalyst. The fresh M / C catalyst enters the methanol reforming chamber 10 through the first U-valve tipper 4 and generates H2 and CO2 under catalytic and reaction conditions for power generation in fuel cells.

[0058] The deactivated M / C catalyst is recycled to the catalyst regeneration combustion chamber 8, and under the conditions of O2 and high temperature, the M of the M / C catalyst undergoes surface exchange with O2, and the oxygen ions are further transferred to the M lattice to form a stable MO x , to activate the catalytic active components, C burns to generate heat; then it is fed into the biomass chemical chain carbonization reactor 9 through the second U-valve turner 11;

[0059] The synthesis gas stream generated in the biomass chemical chain carbonization reactor 9 is partially recycled to the bottom catalyst regeneration combustion chamber 8 to achieve energy cascade utilization.

[0060] In the reactor, the present invention realizes biomass chemical chain carbonization, biomass energy cascade utilization, CO2 gas capture and methanol steam reforming catalyst preparation and regeneration by releasing lattice oxygen. The chemical chain cycle process is as follows: Figure 3 shown.

[0061] Example 1

[0062] 1. Biomass and oxygen carrier CuO are introduced into biomass chemical chain carbonization reactor 9 to obtain synthesis gas and Cu / C. The temperature of biomass chemical chain carbonization reactor 9 is controlled at 320°C. The distribution of the obtained products is as follows: Figure 4 As shown;

[0063] 2. The fresh Cu / C obtained in step 1 is introduced into the methanol reforming chamber 10 through the first U-valve turner 4 to catalyze the methanol steam reforming reaction to produce H2 and CO2. The temperature of the methanol reforming chamber 10 is controlled at 240°C. The methanol conversion rate is as follows: Figure 5 As shown, the hydrogen atom utilization rate is Figure 6 The product distribution is shown in Figure 7 shown.

[0064] 3. The Cu / C catalyst deactivated in step 2 and the synthesis gas obtained in step 1 are introduced into the catalyst regeneration combustion chamber 8 to react to obtain CuO, CO2 and water vapor. The temperature of the catalyst regeneration combustion chamber 8 is controlled at 350°C.

[0065] Example 2

[0066] 1. Biomass and oxygen carrier CuO are introduced into a biomass chemical chaining carbonization reactor 9 to obtain synthesis gas and Cu / C. The temperature of the biomass chemical chaining carbonization reactor 9 is controlled at 300° C.

[0067] 2. The fresh Cu / C obtained in step 1 is introduced into the methanol reforming chamber 10 through the first U-valve tipper 4 to catalyze the methanol steam reforming reaction to produce H2 and CO2. The temperature of the methanol reforming chamber 10 is controlled at 220°C.

[0068] 3. The Cu / C catalyst deactivated in step 2 and the synthesis gas obtained in step 1 are introduced into the catalyst regeneration combustion chamber 8 to react to obtain CuO, CO2 and water vapor. The temperature of the catalyst regeneration combustion chamber 8 is controlled at 370°C.

[0069] Example 3

[0070] 1. Biomass and oxygen carrier CuO are introduced into a biomass chemical chaining carbonization reactor 9 to obtain synthesis gas and Cu / C. The temperature of the biomass chemical chaining carbonization reactor 9 is controlled at 280°C.

[0071] 2. The fresh Cu / C obtained in step 1 is introduced into the methanol reforming chamber 10 through the first U-valve tipper 4 to catalyze the methanol steam reforming reaction to produce H2 and CO2. The temperature of the methanol reforming chamber 10 is controlled at 200°C.

[0072] 3. The Cu / C catalyst deactivated in step 2 and the synthesis gas obtained in step 1 are introduced into the catalyst regeneration combustion chamber 8 to react to obtain CuO, CO2 and water vapor. The temperature of the catalyst regeneration combustion chamber 8 is controlled at 390°C.

[0073] Example 4

[0074] 1. Biomass and oxygen carrier CuO are introduced into a biomass chemical chaining carbonization reactor 9 to obtain synthesis gas and Cu / C. The temperature of the biomass chemical chaining carbonization reactor 9 is controlled at 260°C.

[0075] 2. The fresh Cu / C obtained in step 1 is introduced into the methanol reforming chamber 10 through the first U-valve tipper 4 to catalyze the methanol steam reforming reaction to produce H2 and CO2. The temperature of the methanol reforming chamber 10 is controlled at 260°C.

[0076] 3. The Cu / C catalyst deactivated in step 2 and the synthesis gas obtained in step 1 are introduced into the catalyst regeneration combustion chamber 8 to react to obtain CuO, CO2 and water vapor. The temperature of the catalyst regeneration combustion chamber 8 is controlled at 410°C.

[0077] Example 5

[0078] 1. Biomass and oxygen carrier CuO are introduced into a biomass chemical chaining carbonization reactor 9 to obtain synthesis gas and Cu / C. The temperature of the biomass chemical chaining carbonization reactor 9 is controlled at 240°C.

[0079] 2. The fresh Cu / C obtained in step 1 is introduced into the methanol reforming chamber 10 through the first U-valve tipper 4 to catalyze the methanol steam reforming reaction to produce H2 and CO2. The temperature of the methanol reforming chamber 10 is controlled at 280°C.

[0080] 3. The Cu / C catalyst deactivated in step 2 and the synthesis gas obtained in step 1 are introduced into the catalyst regeneration combustion chamber 8 to react to obtain CuO, CO2 and water vapor. The temperature of the catalyst regeneration combustion chamber 8 is controlled at 430°C.

[0081] Example 6

[0082] 1. Biomass and oxygen carrier CuO are introduced into a biomass chemical chaining carbonization reactor 9 to obtain synthesis gas and Cu / C. The temperature of the biomass chemical chaining carbonization reactor 9 is controlled at 350° C.

[0083] 2. The fresh Cu / C obtained in step 1 is introduced into the methanol reforming chamber 10 through the first U-valve tipper 4 to catalyze the methanol steam reforming reaction to produce H2 and CO2. The temperature of the methanol reforming chamber 10 is controlled at 300°C.

[0084] 3. The Cu / C catalyst deactivated in step 2 and the synthesis gas obtained in step 1 are introduced into the catalyst regeneration combustion chamber 8 to react to obtain CuO, CO2 and water vapor. The temperature of the catalyst regeneration combustion chamber 8 is controlled at 450°C.

[0085] The above embodiments are only preferred implementations of the present invention. It should be pointed out that in the above embodiments, CuO is used as a circulating oxygen carrier, and for RuO2 / Rh2O3 / PdO, it falls within the protection scope of the present invention. For ordinary technicians in this technical field, without departing from the principles of the present invention, several improvements and equivalent substitutions can be made. These technical solutions after improvements and equivalent substitutions to the claims of the present invention all fall within the protection scope of the present invention.

Claims

1. A biomass chemical chain carbonization catalytic material preparation and co-production of hydrogen device, characterized in that: The reactor (7) comprises an air distribution plate (5) provided in the reactor (7), and the air distribution plate (5) divides the inner cavity of the reactor (7) into an upper biomass chemical chain carbonization reactor (9) and a lower catalyst regeneration combustion chamber (8); Biomass chemical chain carbonization reactor (9) using MO x Lattice oxygen realizes biomass carbonization, while MO x Reduction, and the generated M particles are uniformly supported on the surface of biochar to form M / C catalyst; The high-temperature gas carrying heat generated by the combustion in the catalyst regeneration combustion chamber (8) enters the biomass chemical chain carbonization reactor (9) upward through the air distribution plate (5), providing heat energy for the biomass carbonization reaction; the catalyst regeneration combustion chamber (8) is also used to activate the spent M / C catalyst into MO x ; The top feed port of the biomass chemical chain carbonization reactor (9) is connected to a screw feeder (6) for the biomass to enter; The bottom discharge port of the biomass chemical chain carbonization reactor (9) is connected to the feed port of the methanol reforming chamber (10) through the first U-valve turner (4), providing the methanol reforming chamber (10) with fresh M / C catalyst for methanol hydrogen production; The discharge port of the methanol reforming chamber (10) is connected to the feed port of the catalyst regeneration combustion chamber (8); the spent M / C catalyst in the methanol reforming chamber (10) enters the catalyst regeneration combustion chamber (8); The discharge port of the catalyst regeneration combustion chamber (8) is connected to the circulation inlet at the top of the biomass chemical chain carbonization reactor (9) through the second U-valve turner (11), and the MO x The biomass is fed into a biomass chemical chain carbonization reactor (9); The top exhaust port of the biomass chemical chain carbonization reactor (9) is connected to the feed port of the catalyst regeneration combustion chamber (8) through an air inlet system, and the synthesis gas generated by the biomass chemical chain carbonization is supplied to the catalyst regeneration combustion chamber (8); the feed port of the catalyst regeneration combustion chamber (8) is also supplied with oxygen through the air inlet system.

2. The biomass chemical chain carbonization catalytic material preparation and hydrogen co-production device according to claim 1 is characterized in that: The air intake system comprises an air pump (1), a pressure reducing valve (2) and a flow meter (3) which are connected in sequence.

3. A method for preparing and co-producing hydrogen by using biomass chemical chain carbonization catalytic materials, characterized in that: A device for co-producing hydrogen is prepared using the biomass chemical chaining carbonization catalytic material according to claim 1 or 2, wherein the method comprises the following steps: The biomass is fed to the biomass chemical chain carbonization reactor (9) by a screw feeder (6) and mixed with MO x At the same time, they fall in and react at high temperature to generate biosynthesis gas, while the biomass is carbonized to generate biochar; MO in biomass chemical chain carbonization reactor (9) x The catalyst is reduced to M particles and highly dispersed on the biochar material to form a fresh M / C catalyst. The fresh M / C catalyst enters the methanol reforming chamber (10) through the first U-valve turner (4) and generates H2 and CO2 under catalytic and reaction conditions for power generation in fuel cells. The deactivated M / C catalyst is recycled to the catalyst regeneration combustion chamber (8), and under the conditions of O2 and high temperature, the M of the M / C catalyst undergoes surface exchange with O2, and the oxygen ions are further transferred to the M lattice to form a stable MO x , activating the catalytic active components, causing C to burn and generate heat; and then being fed into the biomass chemical chain carbonization reactor (9) through the second U-valve turner (11); The synthesis gas flow generated in the biomass chemical chain carbonization reactor (9) is partially recycled to the bottom catalyst regeneration combustion chamber (8) to achieve energy cascade utilization.

4. The method for preparing and co-producing hydrogen by using a biomass chemical chaining carbonization catalytic material according to claim 3, characterized in that: The biomass carbonization reaction temperature in the biomass chemical chain carbonization reactor (9) is 200-350°C.

5. The method for preparing and co-producing hydrogen by using biomass chemical chaining carbonization catalytic materials according to claim 3, characterized in that: The reaction temperature of the catalyst regeneration combustion chamber (8) is 350-450°C.

6. The method for preparing and co-producing hydrogen by using biomass chemical chaining carbonization catalytic materials according to claim 3, characterized in that: The methanol steam reforming reaction temperature in the methanol reforming chamber (10) ranges from 200 to 300°C.

7. The method for preparing and co-producing hydrogen by using biomass chemical chaining carbonization catalytic materials according to claim 3, characterized in that: The MO x and M / C catalysts, wherein M is Cu, Pd, Ru or Rh.

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