A method for preparing deoxygenated oil and carbon materials with high specific surface area from energy-saving biomass

Abstract

The present invention discloses a method for preparing deoxygenated oil and carbon materials with high specific surface area in an energy-saving manner. The method includes treatment steps such as pressurized pyrolysis, in-situ activation, one-step activation trapping conversion for deoxygenation, and incineration. Biomass is subjected to pressurized pyrolysis in different temperature ranges in a pressurized pyrolysis unit to obtain pyrolysis coke, pyrolysis steam, and pyrolysis volatiles. The pyrolysis steam is used for in-situ activation of pyrolysis coke to prepare activated carbon with high specific surface area, and activated syngas is obtained. The activated carbon with high specific surface area is introduced into an active component aerosol, and at the same time, a catalytic reforming reaction for one-step activation trapping conversion for deoxygenation of biomass pyrolysis volatiles is carried out to obtain a biomass carbon-based catalyst, syngas, and high-quality deoxygenated oil. The activated syngas and the syngas are incinerated in an incineration unit to recover energy, which is used to supply energy to the pressurized pyrolysis unit and the activation unit, and finally, low-temperature flue gas is discharged. This method not only solves the problem of high energy consumption in biomass resource utilization but also provides a technical solution for improving the quality of biomass pyrolysis products.

Description

Technical Field:

[0001] The present invention relates to the technical field of biomass pyrolysis and improvement of pyrolysis product quality, and specifically relates to a method for preparing deoxygenated oil and carbon materials with high specific surface area from energy-saving biomass. Background Art:

[0002] Biomass renewable resources play an important role in the energy structure, and the proportion in the total energy consumption structure is increasing year by year. There are problems in biomass pyrolysis such as many pollutant components in the crude pyrolysis gas, high oxygen content in the pyrolysis oil, poor quality of the pyrolysis coke, and high pyrolysis energy consumption. It is necessary to improve the quality of biomass pyrolysis products and reduce energy consumption. Summary of the Invention:

[0003] Aiming at the problem that biomass cannot be effectively resourceized with low energy consumption in the above-mentioned prior art, the present invention provides a method for preparing deoxygenated oil and carbon materials with high specific surface area from energy-saving biomass. The deoxygenated oil (deoxygenated bio-oil) and carbon materials obtained by this method have high quality, the oxygen content in the bio-oil is reduced, the specific surface area of the carbon materials is increased, the particles are uniform and of good quality, and the pollutant concentration in the incineration flue gas is low.

[0004] The purpose of the present invention is to provide a method for preparing deoxygenated oil and carbon materials with high specific surface area from energy-saving biomass. According to the large difference in the thermal stability of different components of biomass, the biomass is subjected to stepwise pressurized pyrolysis, activation, capture and conversion, and incineration in different temperature sections in sequence to obtain a carbon-based catalyst (10), deoxygenated oil (12) and low-temperature flue gas (13). The specific steps are as follows: The biomass (1) is respectively fed into a primary pressurized pyrolysis unit and a secondary pressurized pyrolysis unit for pressurized pyrolysis in different temperature sections to obtain pyrolysis water vapor (6), pyrolysis volatile matter (2) / (3) and pyrolysis coke (4) / (5); The pyrolysis water vapor (6) respectively passes through an in-situ activation unit to perform in-situ activation on the pyrolysis coke (4) / (5) to obtain high-specific-surface-area activated carbon (7) and activated syngas (8); The high-specific-surface-area activated carbon (7) enters a one-step activation capture conversion deoxygenation unit and reacts with the pyrolysis volatile matter (2)(3) in the atmosphere of an active component aerosol (9) through activation catalytic reforming reaction to obtain a carbon-based catalyst (10), syngas (11) and deoxygenated oil (12); The activated syngas (8) and the syngas (11) enter an incineration unit for incineration to provide energy for the primary pressurized pyrolysis unit, the secondary pressurized pyrolysis unit and the in-situ activation unit, and obtain low-temperature flue gas (13), realizing low-energy consumption resourceization of biomass.

[0005] According to the large difference in the thermal stability of different components of biomass, the biomass is pyrolyzed at different temperature ranges to obtain pyrolysis water vapor, pyrolysis gas, condensed pyrolysis oil, and pyrolysis char. The condensed pyrolysis oil and pyrolysis char are the main products of biomass pyrolysis, and the improvement of their quality and recycling determine the economy of biomass pyrolysis. The biomass pyrolysis water vapor is used for the in-situ activation of pyrolysis char to prepare activated carbon with a high specific surface area, which is used for the adsorption treatment of heavy metals in sewage and VOCs in the air, and can also be used in fields such as catalysts and energy storage materials. The active component aerosol performs one-step activation capture conversion and deoxidation on the activated carbon with a high specific surface area and pyrolysis volatiles, and the obtained carbon-based catalyst can be used to improve the quality of biomass oil.

[0006] Preferably, the pyrolysis water vapor (6) obtained from the primary pressurized pyrolysis unit and the secondary pressurized pyrolysis unit is collected in the same container; the deoxygenated oil (12) and the carbon-based catalyst (10) obtained by pressurized pyrolysis, in-situ activation, and one-step activation capture conversion and deoxidation of the biomass are respectively collected in the same container.

[0007] Preferably, the biomass passes through the primary / secondary pressurized pyrolysis unit, with a nitrogen gas flow rate of 100 - 200 mL / min, a pressure of 0.1 - 35 MPa, and a temperature of 150°C - 200°C for 0.5 - 1.0 h to obtain pyrolysis water vapor (6), and then the temperature is raised to 500°C - 650°C and maintained for 0.8 - 1.5 h to obtain pyrolysis volatiles (2) / (3) and pyrolysis char (4) / (5).

[0008] Preferably, the pyrolysis water vapor (6) enters the in-situ activation unit III / IV to in-situ activate the high-temperature pyrolysis char (4) / (5) to obtain activated carbon with a high specific surface area (7) and activated syngas (8). In the in-situ activation unit III / IV, the activation pressure is 0.1 - 35 MPa, the activation temperature is 550°C - 1000°C, the activation time is 0.5 - 1.0 h, and the mass ratio of the pyrolysis water vapor (6) to the pyrolysis char (4) / (5) is 0.1 - 0.8. The low-temperature flue gas (13) also provides energy for the in-situ activation unit III / IV.

[0009] The pyrolysis water vapor obtained from the secondary pressurized pyrolysis unit serves as a reactant in the in-situ activation unit III, and the pyrolysis water vapor obtained from the primary pressurized pyrolysis unit serves as a reactant in the in-situ activation unit IV, enabling the full utilization of the products obtained from the pyrolysis reaction.

[0010] Preferably, the specific surface area of the activated carbon with a high specific surface area (7) obtained by in-situ activation is 100 - 1200 m 2 / g, and the ash concentration is 0.1 - 2.0 wt.%.

[0011] Preferably, the high specific surface area activated carbon (7) and the pyrolysis volatiles of biomass (2) / (3) are introduced into the activation capture conversion deoxygenation unit in the atmosphere of the active component aerosol (9) to carry out activation catalytic reforming reaction, obtaining a carbon-based catalyst (10), synthesis gas (11) and deoxygenated oil (12). The reaction temperature is 550°C to 900°C, the reaction pressure is 0.1 to 35 MPa, the reaction time is 0.5 to 2.0 h, the mass ratio of the pyrolysis volatiles (2) / (3) to the high specific surface area activated carbon (7) is 0.5 to 5.0, the mass concentration of the active component in the active component aerosol is 10% to 50%, and the mass ratio of the active component aerosol to the high specific surface area activated carbon is 0.01 to 0.20. Further preferably, the reaction temperature is 600°C to 650°C, the reaction time is 1.0 to 1.5 h, the mass ratio of the pyrolysis volatiles (2) / (3) to the high specific surface area activated carbon (7) is 1.5 to 3.0, the mass concentration of the active component in the active component aerosol is 10% to 15%, and the mass ratio of the active component aerosol (9) to the high specific surface area activated carbon (7) is 0.05 to 0.10.

[0012] Preferably, the active component in the active component aerosol is a metal oxide, including CaO, Fe2O3, MaO, K2O and BaO.

[0013] Preferably, the activated synthesis gas (8) obtained by in-situ activation and the synthesis gas (11) obtained by activation capture conversion deoxygenation are incinerated to obtain low-temperature flue gas (13) to supply energy to the pressurized pyrolysis unit and the in-situ activation unit, and the incineration temperature is 700°C to 1000°C.

[0014] Preferably, in the low-temperature flue gas (13), the emission concentrations of SO x (sulfur oxides) and NO x (nitrogen oxides) are respectively lower than 20 mg / m 3 and 30 mg / m 3 . Further preferably, the SO x emission concentration is 0.1 to 15 mg / m 3 , and the NO x emission concentration is 0.1 to 20 mg / m 3 .

[0015] The pyrolysis volatiles (2) / (3), the high specific surface area activated carbon (7) obtained by in-situ activation and the metal oxide aerosol enter the one-step activation capture conversion deoxygenation unit V at the same time to improve the quality of the pyrolysis volatiles (2) / (3) and the high specific surface area activated carbon (7), obtaining a carbon-based catalyst (10), synthesis gas (11) and deoxygenated oil (12). The specific surface area of the carbon-based catalyst (10) is 100 to 1000 m 2 / g, the ash concentration is 0.1 to 3.0 wt.%. The CO2 concentration in the received syngas (11) is 1% to 10%, and the NO x (nitrogen oxides) concentration is 0.01% to 0.09%, and the SO x (sulfur oxides) concentration is 0.01% to 0.09%. The hydrogen concentration is 5% to 20%, the methane concentration is 20% to 45%, the CO concentration is 15% to 35%, and the oxygen content concentration in the deoxygenated oil (12) is 0.1% to 1.0%.

[0016] Compared with the prior art, the present invention has the following advantages: By the method for energy-saving preparation of deoxygenated oil and high specific surface area carbon materials of the present invention, low-concentration deoxygenated oil, carbon-based catalyst and low-temperature flue gas are prepared, and at the same time, the energy consumption of biomass pyrolysis treatment is reduced. The oxygen content concentration in the deoxygenated oil prepared by the present invention is low and can be used as a liquid fuel to replace fossil fuels. The carbon-based catalyst prepared by the present invention has a large specific surface area, uniform particles and good quality, and can be used as a de-O / S / N catalyst for biomass pyrolysis oil. The pollutant emission concentration in the low-temperature flue gas emitted by the present invention is low. The present invention not only solves the problem of high energy consumption in biomass treatment, but also provides a way for the resource recycling of biomass, and has broad application prospects. Brief Description of the Drawings:

[0017] Figure 1 It is a process schematic diagram for the energy-saving preparation of deoxygenated oil and high specific surface area carbon materials from biomass according to the present invention. Detailed Embodiments:

[0018] The following examples are further descriptions of the present invention, rather than limitations of the present invention.

[0019] Unless otherwise defined, all professional terms used hereinafter have the same meaning as commonly understood by those skilled in the art. The professional terms used herein are only for the purpose of describing specific embodiments and are not intended to limit the protection scope of the present invention. Unless otherwise specified, the experimental materials and reagents in this article are all conventional commercially available products in this technical field. The biomass proposed by the present invention includes straw, sawdust, bagasse, rice bran, etc. In the following examples, the preferred biomass is corn straw. The particle size of the biomass after crushing is more than 100 mesh.

[0020] Example 1

[0021] See Figure 1 , a method for energy-saving preparation of deoxygenated oil and high specific surface area carbon materials from biomass. According to the large difference in the thermal stability of different components of biomass, the biomass is subjected to stepwise pressurized pyrolysis activation capture conversion and incineration at different temperature sections to obtain a carbon-based CaO catalyst, deoxygenated oil (12) and low-temperature flue gas (13). The method specifically includes the following steps:

[0022] (1) Due to the large difference in thermal stability among different components of biomass, the crushed biomass is fed into the first-stage pressurized pyrolysis unit I for pressurized pyrolysis at different temperature ranges, obtaining pyrolysis volatiles (2), pyrolysis water vapor (6), and pyrolysis char (4). The height of the biomass filler does not exceed 3 / 5 of the furnace body of the first-stage pressurized pyrolysis unit I. First, at a nitrogen flow rate of 200 mL / min, a pressure of 1.0 MPa, and a temperature of 200 °C for 0.5 h, pyrolysis water vapor (6) is obtained. Then, the temperature is raised to 600 °C and maintained for 1.0 h to obtain pyrolysis volatiles (2) and pyrolysis char (4).

[0023] (2) Due to the large difference in thermal stability among different components of biomass, the crushed biomass is fed into the second-stage pressurized pyrolysis unit II for pressurized pyrolysis at different temperature ranges. The height of the biomass filler does not exceed 3 / 5 of the furnace body of the second-stage pressurized pyrolysis unit. First, at a nitrogen flow rate of 200 mL / min, a pressure of 1.0 MPa, and a temperature of 200 °C for 0.5 h, pyrolysis water vapor (6) is obtained. The pyrolysis water vapor (6) is introduced into the in-situ activation unit III, and the pyrolysis char (4) is in-situ activated at 600 °C and 1.0 MPa for 1.0 h to obtain high specific surface area activated carbon (7) and activated syngas (8). The mass ratio of pyrolysis water vapor (6) to pyrolysis char (4) is 0.5. The specific surface area of the high specific surface area activated carbon is 800 m 2 / g.

[0024] (3) The temperature of the second-stage pressurized pyrolysis unit II is raised to 600 °C and maintained for 1.0 h to obtain pyrolysis volatiles (3) and pyrolysis char (5). The pyrolysis volatiles (3), 13.0% CaO aerosol at 300 °C, and high specific surface area activated carbon (7) simultaneously enter the one-step activation capture conversion deoxidation unit V, and a catalytic reforming reaction is carried out at 600 °C for 2.0 h. The mass ratio of high specific surface area activated carbon (7) to pyrolysis volatiles (3) is 3.0, and the mass ratio of CaO aerosol to high specific surface area activated carbon (7) is 0.05, obtaining a biomass carbon-based CaO catalyst, syngas (11), and deoxidized oil (12). The specific surface area of the biomass carbon-based CaO catalyst is 500 m 2 / g, the ash concentration is 1.0 wt.%, and the oxygen content of the deoxidized oil (12) is 0.5%. The CO2 concentration in the syngas (11) is 2.0%, NO x concentration is 0.03%, SO x concentration is 0.02%, the hydrogen concentration is 8%, the methane concentration is 30%, and the CO concentration is 28%.

[0025] (4) The activated syngas (8) and syngas (11) are introduced into the incineration unit VI and incinerated at 700 °C to obtain low-temperature flue gas (13). The heat energy generated by incineration is used to supply energy to the primary pressurized pyrolysis unit I, the secondary pressurized pyrolysis unit II, and the in-situ activation unit III. The SO2 emission concentration in the discharged low-temperature flue gas (13) is 10 mg / m 3 , NO x emission concentration is 15 mg / m 3 .

[0026] Example 2

[0027] See Figure 1 , a method for preparing deoxygenated oil and carbon-based catalyst from energy-saving biomass. According to the large difference in thermal stability of different components of biomass, the biomass is subjected to stepwise pyrolysis activation capture conversion incineration at different temperature segments to obtain carbon-based MgO catalyst, deoxygenated oil (12), and low-temperature flue gas (13). This method specifically includes the following steps:

[0028] (1) According to the large difference in thermal stability of different components of biomass, the crushed biomass is sent to the secondary pressurized pyrolysis unit II for pyrolysis at different temperature segments to obtain pyrolysis volatiles (3), pyrolysis water vapor (6), and pyrolysis coke (5). The height of the biomass filler does not exceed 2 / 3 of the furnace body of the secondary pressurized pyrolysis unit II. First, at a nitrogen flow rate of 150 mL / min, a pressure of 2.0 MPa, and a temperature of 150 °C for 1.0 h, pyrolysis water vapor (6) is obtained. Then, the temperature is raised to 650 °C and maintained for 0.8 h to obtain pyrolysis volatiles (3) and pyrolysis coke (5).

[0029] (2) According to the large difference in thermal stability of different components of biomass, the crushed biomass is sent to the primary pressurized pyrolysis unit I for pyrolysis at different temperature segments. The height of the biomass filler does not exceed 2 / 3 of the furnace body of the primary pressurized pyrolysis unit. First, at a nitrogen flow rate of 150 mL / min, a pressure of 2.0 MPa, and a temperature of 150 °C for 1.0 h, pyrolysis water vapor (6) is obtained. The pyrolysis water vapor (6) is introduced into the in-situ activation unit IV and in-situ activated with pyrolysis coke (5) for 0.5 h at 600 °C and 2.0 MPa to obtain high specific surface area activated carbon (7) and activated syngas (8). The specific surface area of the high specific surface area activated carbon (7) is 600 m 2 / g.

[0030] (3) Raise the temperature of the primary pressurized pyrolysis unit I to 650 °C and maintain it for 0.8 h to obtain pyrolysis volatiles (3) and pyrolysis coke (5). The pyrolysis volatiles (3), 15.0% MgO aerosol at 250 °C, and high specific surface area activated carbon (7) simultaneously enter the one-step activation capture conversion deoxidation unit V, and a catalytic reforming reaction is carried out at 650 °C for 0.5 h. The mass ratio of the high specific surface area activated carbon to the pyrolysis volatiles (3) is 1.5, and the mass ratio of the MgO aerosol to the high specific surface area activated carbon is 0.08, to obtain a carbon-based MgO catalyst, syngas (11), and deoxygenated oil (12). The specific surface area of the carbon-based MgO catalyst is 450 m 2 / g, the ash concentration is 2.0 wt.%, and the oxygen content of the deoxygenated oil (12) is 0.9%. The CO2 concentration in the syngas (11) is 5.0%, NO x concentration is 0.09%, SO x concentration is 0.06%, the hydrogen concentration is 10%, the methane concentration is 35%, and the CO concentration is 20%.

[0031] (4) The activated syngas (8) and the syngas (11) are introduced into the incineration unit VI and incinerated at 750 °C to obtain low-temperature flue gas (13). The heat energy generated by the incineration is used to supply energy to the primary pressurized pyrolysis unit I and the secondary pressurized pyrolysis unit II. The SO2 emission concentration in the discharged low-temperature flue gas (13) is 16 mg / m 3 , NO x emission concentration is 10 mg / m 3 .

[0032] Example 3

[0033] See Figure 1 , a method for preparing deoxygenated oil and carbon-based catalyst from energy-saving biomass. According to the large difference in the thermal stability of different components of biomass, the biomass is subjected to stepwise pyrolysis, activation, capture, conversion, and incineration at different temperature segments to obtain a biomass-based BaO catalyst, deoxygenated oil (12), and low-temperature flue gas (13). This method specifically includes the following steps:

[0034] (1) According to the large difference in the thermal stability of different components of biomass, the crushed biomass is sent to the primary pressurized pyrolysis unit I for pyrolysis at different temperature segments to obtain pyrolysis volatiles (2), pyrolysis water vapor (6), and pyrolysis coke (4). The height of the biomass filler does not exceed 3 / 5 of the furnace body of the primary pressurized pyrolysis unit I. First, at a nitrogen flow rate of 100 mL / min, a pressure of 0.5 MPa, and a temperature of 200 °C, it is maintained for 1.0 h to obtain pyrolysis water vapor (6). Then, the temperature is raised to 650 °C and maintained for 1.5 h to obtain pyrolysis volatiles (2) and pyrolysis coke (4).

[0035] (2) According to the significant difference in the thermal stability of different components of biomass, the crushed biomass is fed into the secondary pressurized pyrolysis unit II for pyrolysis at different temperature ranges. The height of the biomass does not exceed 3 / 5 of the furnace body of the secondary pressurized pyrolysis unit. First, under the conditions of a nitrogen flow rate of 100 mL / min, a pressure of 0.5 MPa, and a temperature of 200 °C for 1.0 h, pyrolysis water vapor (6) is obtained. The pyrolysis water vapor (6) is introduced into the in-situ activation unit III, and the pyrolysis char (4) is in-situ activated at 650 °C and 0.5 MPa for 1.0 h to obtain high specific surface area activated carbon (7) and activated syngas (8). The specific surface area of the high specific surface area activated carbon (7) is 850 m 2 / g.

[0036] (3) The temperature of the secondary pressurized pyrolysis unit II is raised to 650 °C and maintained for 1.5 h to obtain pyrolysis volatiles (3) and pyrolysis char (5). The pyrolysis volatiles (3), 10.0% BaO aerosol at 300 °C, and the high specific surface area activated carbon (7) simultaneously enter the one-step activation, capture, conversion, and deoxygenation unit V, and a catalytic reforming reaction is carried out at 650 °C for 1.0 h. The mass ratio of the high specific surface area activated carbon to the pyrolysis volatiles (3) is 3.0, and the mass ratio of the active component aerosol to the high specific surface area activated carbon is 0.10, to obtain a carbon-based BaO catalyst, syngas (11), and deoxygenated oil (12). The specific surface area of the carbon-based BaO catalyst (10) is 400 m 2 / g, the ash concentration is 1.5 wt.%, and the oxygen content of the deoxygenated oil (12) is 0.3%. The CO2 concentration in the syngas (11) is 5.0%, NO x concentration is 0.06%, SO x concentration is 0.09%, the hydrogen concentration is 15%, the methane concentration is 25%, and the CO concentration is 23%.

[0037] (4) The activated syngas (8) and the syngas (11) are introduced into the incineration unit VI and incinerated at 800 °C to obtain low-temperature flue gas (13). The heat energy generated by the incineration is used to supply energy to the primary pressurized pyrolysis unit I and the secondary pressurized pyrolysis unit II. The SO2 emission concentration in the discharged low-temperature flue gas (13) is 10 mg / m 3 , NO x emission concentration is 25 mg / m 3 .

[0038] The description of the above embodiments is only used to help understand the technical solution and its core idea of the present invention. It should be noted that for those skilled in the art of this technology, without departing from the principle of the present invention, several improvements and modifications can still be made to the present invention, and these improvements and modifications also fall within the protection scope of the claims of the present invention.

Claims

1. A method for preparing deoxygenated oil and carbon materials with high specific surface area from energy-saving biomass, characterized in that: According to the large difference in the thermal stability of different components of biomass, biomass is subjected to stepwise pressurized pyrolysis, activation, capture conversion, and incineration at different temperature stages to obtain a carbon-based catalyst (10), deoxygenated oil (12), and low-temperature flue gas (13); specifically, the following steps are included: Biomass (1) is separately fed into a primary pressurized pyrolysis unit and a secondary pressurized pyrolysis unit for pressurized pyrolysis at different temperature stages to obtain pyrolysis water vapor (6), pyrolysis volatiles (2) / (3), and pyrolysis coke (4) / (5); the pyrolysis water vapor (6) is respectively used to in-situ activate the pyrolysis coke (4) / (5) through an in-situ activation unit to obtain high-specific-surface-area activated carbon (7) and activated syngas (8); the high-specific-surface-area activated carbon (7) enters a one-step activation capture conversion deoxygenation unit and undergoes a catalytic reforming reaction with the pyrolysis volatiles (2) / (3) in an active component aerosol (9) atmosphere to obtain a carbon-based catalyst (10), syngas (11), and deoxygenated oil (12); the activated syngas (8) and the syngas (11) enter an incineration unit for incineration, and after providing energy for the primary pressurized pyrolysis unit, the secondary pressurized pyrolysis unit, and the in-situ activation unit, low-temperature flue gas (13) is obtained, realizing the low-energy-consumption resource utilization of biomass; the biomass passes through the primary / secondary pressurized pyrolysis unit, and at a nitrogen flow rate of 100 - 200 mL / min, a pressure of 0.1 - 35 MPa, and a temperature of 150 °C - 200 °C, it is maintained for 0.5 - 1.0 h to obtain pyrolysis water vapor (6), and then the temperature is raised to 500 °C - 650 °C and maintained for 0.8 - 1.5 h to obtain pyrolysis volatiles (2) / (3) and pyrolysis coke (4) / (5).

2. The method according to claim 1, characterized in that: The pyrolysis water vapor (6) obtained from the primary pressurized pyrolysis unit and the secondary pressurized pyrolysis unit is collected in the same container; the deoxygenated oil (12) and the carbon-based catalyst (10) obtained by the biomass through pressurized pyrolysis, in-situ activation, and one-step activation capture conversion deoxygenation are respectively collected in the same container.

3. The method according to claim 1 or 2, characterized in that: The pyrolysis water vapor (6) obtained by the low-temperature pyrolysis of biomass enters the in-situ activation unit III / IV to in-situ activate the high-temperature pyrolysis coke (4) / (5) to obtain high-specific-surface-area activated carbon (7) and activated syngas (8). The activation pressure is 0.1 - 35 MPa, the activation temperature is 550 °C - 1000 °C, the activation time is 0.5 - 1.0 h, and the mass ratio of the pyrolysis water vapor (6) to the pyrolysis coke (4) / (5) is 0.1 - 0.

8.

4. The method according to claim 3, wherein: The specific surface area of the high specific surface area activated carbon (7) obtained by in-situ activation is 100 to 1200 m 2 / g, and the ash concentration is 0.1 to 2.0 wt.%.

5. The method according to claim 1, wherein: The high specific surface area activated carbon (7) and the biomass pyrolysis volatiles (2) / (3) are introduced into the one-step activation trapping conversion deoxidation unit with an active component aerosol (9) atmosphere for an activation catalytic reforming reaction to obtain a carbon-based catalyst (10), syngas (11) and deoxygenated oil (12). The reaction temperature is 550 °C to 900 °C, the reaction pressure is 0.1 to 35 MPa, the reaction time is 0.5 to 2.0 h, the mass ratio of the pyrolysis volatiles (2) / (3) to the high specific surface area activated carbon (7) is 0.5 to 5.0, the mass concentration of the active component in the active component aerosol is 10% to 50%, and the mass ratio of the active component aerosol (9) to the high specific surface area activated carbon (7) is 0.01 to 0.

20.

6. The method according to claim 5, wherein: The active component in the active component aerosol (9) is a metal oxide, including CaO, Fe2O3, MaO, K2O and BaO.

7. The method according to claim 5, characterized in that: The oxygen content of the deoxygenated oil (12) obtained by activation, capture, and conversion deoxygenation is 0.1 to 1.0%, and the specific surface area of the carbon-based catalyst (10) obtained by activation, capture, and conversion deoxygenation is 100 to 1000 m 2 / g, and the ash concentration is 0.1 to 3.0 wt.%.

8. The method according to claim 1, wherein: The incineration temperature of the incineration unit is 700 °C to 1000 °C.

9. The method according to claim 8, wherein: The emission concentrations of SO x and NO x in the low-temperature flue gas (13) are respectively lower than 20 mg / m 3 and 30 mg / m 3 .

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