A method for catalytic cracking production of biomass liquid fuel

Abstract

The present invention relates to a method for catalytic cracking production of biomass liquid fuel, and the method is as follows: Take MCM-48 mesoporous molecular sieve and calcine it in a solution impregnated with cobalt salt and metal borate to obtain a molecular sieve catalyst. Take lignin raw material and sugar raw material, dry them, and then carry out temperature-raising microwave cracking in a cracking reaction fluidized bed. The oil and gas are further catalytically cracked by the molecular sieve catalyst, and the oil liquid is recovered by condensation. The oil liquid, hydrogen-supplying mixed solvent and Ru / C catalyst are subjected to hydrodeoxygenation, and centrifuged for supercritical extraction and upgrading. The material at the top of the extraction tower enters a first-stage separation tower and a second-stage separation tower under reduced pressure for continuous reduced-pressure separation to obtain the finished product of biomass liquid fuel. The modified MCM-48 molecular sieve catalyst catalytically cracks biomass lignin raw material and sugar raw material by a two-step method, strengthens the deoxygenation reaction, and then undergoes supercritical extraction and upgrading and reduced-pressure separation, reducing the reaction temperature and acid value of the biomass liquid fuel, and improving the liquid-gas conversion rate, high-carbon-number oil liquid yield and product calorific value.

Description

Technical Field

[0001] The invention relates to a method for producing biomass liquid fuel by cracking and catalysis, and belongs to the technical field of biomass liquid fuel production. Background Art

[0002] As people's demand for energy continues to increase, replacing fossil energy with green biomass energy is an important way to achieve sustainable energy development. Using biomass resources such as crop straw and agricultural processing residues, firewood and forestry processing residues, livestock and poultry manure, industrial organic wastewater and waste residues, urban domestic waste and energy plants to produce liquid fuels can effectively reduce harmful gases, smoke and greenhouse gases, and help improve environmental quality. Biomass is mainly converted into usable energy through biochemical conversion and thermochemical conversion, and biogas digesters are used to decompose methane and carbon dioxide through anaerobic fermentation, or yeast ferments sugars into ethanol. Biological methods have technical defects such as long biochemical reaction time, complex post-processing, and difficult to use by-products, and have a greater impact on biochemical reactions. Chemical processes including combustion, vaporization, liquefaction, hydrogenation and thermal cracking can directly hydrogenate or decompose biomass, which is conducive to simplifying operations and better economy.

[0003] The thermal cracking process is an indirect heating process that decomposes and then recombine hydrocarbons, cracking or decomposing high-boiling point, large-molecule organic substances into lower-molecular substances such as light oil and diesel and other high-priced substances. However, traditional thermal cracking takes a long time to heat biomass raw materials with low thermal conductivity, and it can only be cracked at at least 500-600°C, resulting in limited processing capacity, high operating and energy costs, and rapid thermal cracking products contain a large amount of water and acid value, which affect combustion stability and cannot be mixed with traditional fuels. The oxygen content is low, the reforming removal process is complicated, the liquid oil yield and combustion calorific value are not high, and it is difficult to meet the needs of fuel production and application. Summary of the invention

[0004] The purpose of the present invention is to provide a method for producing biomass liquid fuel by cracking and catalysis in view of the defects of the prior art. The modified MCM-48 molecular sieve catalyst catalytically cracks the biomass lignin raw material and the sugar raw material in a two-step process, and after the hydrodeoxygenation reaction, the supercritical extraction is used for quality improvement and vacuum separation, thereby reducing the reaction temperature and acid value of the biomass liquid fuel, and improving the liquid-to-gas conversion rate, the high carbon number oil yield and the product calorific value.

[0005] The present invention is achieved through the following technical solutions:

[0006] A method for producing biomass liquid fuel by cracking and catalysis, wherein the method is as follows:

[0007] S1: Take MCM-48 mesoporous molecular sieve and immerse it in an equimass ratio solution of cobalt salt and metal borate. After filtration and calcination treatment, a molecular sieve catalyst is obtained. The cobalt salt is cobalt disodium ethylenediaminetetraacetate, and the metal borate is tin borate or molybdenum borate. The calcination temperature is 350 - 450 °C, and the calcination time is 2 - 3 h;

[0008] S2: Take lignin raw materials and sugar raw materials, dry them, and put them into a pyrolysis reaction fluidized bed equipped with a microwave generator. The lignin raw materials and sugar raw materials include one or more of wood, bark, wheat, rice, agricultural and forestry waste, sugarcane, and field vegetables, and the water content is controlled to be less than 20%;

[0009] Under negative pressure anaerobic conditions, heat up and pyrolyze to generate ash and oil-gas. The oil-gas is sent to the catalytic reaction zone on the upper layer of the pyrolysis reaction fluidized bed, and further pyrolyzes under the action of the molecular sieve catalyst, and then condenses and recovers the oil liquid. Collect the ash at the bottom of the bed. The reaction pressure of the pyrolysis reaction fluidized bed is -5.5 to -0.6 Mpa, the reaction temperature is 320 - 385 °C, the microwave power of the microwave generator is 50 - 800 W, the microwave frequency is 500 - 1000 MHz, the pyrolysis time is 3 - 6 h, and the non-condensable gas generated during the condensation of the oil-gas is used for circulation and provides part of the heat for the catalytic pyrolysis reaction fluidized bed;

[0010] S3: Put the oil liquid, hydrogen-supplying mixed solvent, and Ru / C catalyst into a high-pressure reactor for hydrodeoxygenation reaction. The mass ratio of the oil liquid to the hydrogen-supplying mixed solvent is 100:(6 - 15). The hydrogen-supplying mixed solvent is composed of two or more of benzyl alcohol, tetrahydroquinoline, tetrahydrophenanthrene, ethyl acetate, and benzyl benzoate in an equimass ratio. The reaction pressure in the high-pressure reactor is 5 - 8 Mpa, the reaction temperature is 280 - 370 °C. There is a stirrer in the high-pressure reactor that is intermittently opened and the stirring rate is 80 - 150 r / min, and the reaction time is 1 - 2 h;

[0011] Subsequently, centrifuge and take the liquid substance and place it in an extraction tower. The extractant enters the extraction tower for supercritical extraction and upgrading after being pressurized and preheated by a high-pressure pump. The extractant is carbon dioxide or methane, the pressure of the extraction kettle is 4 - 6 Mpa, and the supercritical extraction temperature is 100 - 155 °C;

[0012] The material at the top of the extraction tower is transported through a pipeline and enters the first-stage separation tower and the second-stage separation tower for continuous vacuum separation. The pressure of the first-stage separation tower is 2.1 - 3 Mpa, the temperature is 70 - 110 °C, the pressure of the second-stage separation tower is 1 - 2 Mpa, and the temperature is 65 - 100 °C. The separated extractant enters the storage tank for extraction circulation. The bottom products of the first-stage separation tower and the second-stage separation tower are sent to a water-oil separator for separation, and the obtained single oil phase or oil phase mixture is used as the finished product of biomass liquid fuel. The total acid value of the biomass liquid fuel is 80 - 135 mgKOH / g-1 with a calorific value of 38 - 51 MJ / kg -1 。

[0013] The beneficial effects of the present invention are as follows:

[0014] (1) Using lignin raw materials and sugar raw materials as raw materials and controlling the water content, heating and cracking under negative pressure anaerobic conditions during the cracking process, using microwave assistance to improve the penetration performance and avoid temperature difference gradients. The MCM-48 mesoporous molecular sieve with a three-dimensional helical pore network is acid-modified by cobalt salt and metal borate to obtain EDTA-2NaCO-Sn / Mo-MCM-48. The two-step method can avoid coking deactivation during the catalytic cracking process, extend the catalyst activity and lifespan. The by-product ash can be used to produce solid fuel, the catalyst is convenient for recycling, and various acids are converted into esters, which is beneficial to reducing the reaction temperature, increasing the liquid-gas conversion rate and the yield of high-carbon number oil liquids;

[0015] (2) Through the hydrodeoxygenation reaction with a hydrogen-donating mixed solvent and a Ru / C catalyst in a high-pressure reactor, the C-O bond is broken and the C-H bond is formed to reduce the acid value and the content of oxygenated compounds in the oil liquid, effectively inhibiting the formation of visible coke. By optimizing the conditions, supercritical extraction and upgrading, and pressure reduction separation in a two-stage separation tower are used to separate water and oil to extract a single oil phase or a mixture of oil phases as the finished product of biomass liquid fuel, which is beneficial to improving heat transfer and inhibiting the polymerization and coking reaction of bio-oil. Acids and aldehydes are converted into esters and acetals, reducing the oxygen and acid value of the biomass liquid fuel, which is beneficial to increasing the calorific value of the product. Description of the Drawings

[0016] Figure 1 is the process flow chart of the present invention. Detailed Embodiments

[0017] The following further describes the detailed embodiments of the present invention in conjunction with the drawings and examples.

[0018] Example 1:

[0019] A method for catalytic cracking to produce biomass liquid fuel, wherein the method is as follows:

[0020] S1: Take 2 Kg of MCM-48 mesoporous molecular sieve and immerse it in an equal mass ratio solution of 1 Kg of cobalt salt and 1 Kg of metal borate mixed with water, filter and obtain the molecular sieve catalyst through calcination treatment. The cobalt salt is cobalt salt of ethylenediaminetetraacetic acid disodium, the metal borate is molybdenum borate, the calcination temperature is 365 °C, and the calcination time is 2 h;

[0021] S2: Take 40 kg of lignin raw materials and 60 kg of sugar raw materials, dry them, and put them into a pyrolysis reaction fluidized bed equipped with a microwave generator. The lignin raw materials and sugar raw materials include wood, bark, agricultural and forestry waste such as rice husks and sugarcane, and control the water content to be less than 15%;

[0022] Under negative pressure anaerobic conditions, heat up and pyrolyze to generate ash and oil-gas. The oil-gas is sent to the catalytic reaction zone above the pyrolysis reaction fluidized bed, and further pyrolyzed under the action of a molecular sieve catalyst, and then condensed to recover the oil liquid. Collect the ash at the bottom of the bed. The reaction pressure of the pyrolysis reaction fluidized bed is -3 Mpa, the reaction temperature is 365 °C, the microwave power of the microwave generator is 500 W, the microwave frequency is 800 MHz, the pyrolysis time is 4 h, and the non-condensable gas generated during the condensation of the oil-gas is used for circulation and provides part of the heat for the catalytic pyrolysis reaction fluidized bed;

[0023] S3: Put the oil liquid, hydrogen-donating mixed solvent, and Ru / C catalyst into a high-pressure reactor for hydrodeoxygenation reaction. The mass ratio of the oil liquid to the hydrogen-donating mixed solvent is 100:12. The hydrogen-donating mixed solvent is composed of benzyl alcohol and tetrahydrophenanthrene in an equal mass ratio. The reaction pressure in the high-pressure reactor is 5 Mpa, the reaction temperature is 290 °C. There is a stirrer in the high-pressure reactor that is intermittently opened and the stirring rate is 100 r / min, and the reaction time is 2 h;

[0024] Subsequently, centrifuge and take the liquid product and place it in an extraction tower. The extractant enters the extraction tower for supercritical extraction and upgrading after being pressurized and preheated by a high-pressure pump. The extractant is carbon dioxide, the pressure of the extraction kettle is 5 Mpa, and the supercritical extraction temperature is 120 °C;

[0025] S4: The materials at the top of the extraction tower are transported through pipelines into a first-stage separation tower and a second-stage separation tower under reduced pressure for continuous reduced-pressure separation. The pressure of the first-stage separation tower is 2.5 Mpa and the temperature is 85 °C. The pressure of the second-stage separation tower is 1.3 Mpa and the temperature is 78 °C. The separated extractant enters the storage tank for extraction circulation. The bottom products of the first-stage separation tower and the second-stage separation tower are sent to a water-oil separator for separation respectively. The obtained single oil phase is used as the finished product of the biomass liquid fuel. The total acid values of the biomass liquid fuels in the first-stage separation tower and the second-stage separation tower are 112 mg KOH / g -1 、95 mg KOH / g -1 ,and the calorific values are 42 MJ / kg -1 、50 MJ / kg -11 .

[0026] Example 2:

[0027] A method for catalytic pyrolysis to produce biomass liquid fuel, wherein the method is as follows:

[0028] S1: Take 2 Kg of MCM-48 mesoporous molecular sieve and immerse it in an equal mass ratio solution of 1 Kg of cobalt salt and 1 Kg of metal borate in water. Filter and obtain the molecular sieve catalyst through calcination treatment. The cobalt salt is cobalt disodium ethylenediaminetetraacetate, and the metal borate is tin borate. The calcination temperature is 410 °C and the calcination time is 2 h.

[0029] S2: Take 50 kg of lignin raw material and 50 kg of sugar raw material, dry them, and put them into a pyrolysis reaction fluidized bed equipped with a microwave generator. The lignin raw material and sugar raw material include wheat and Hetian vegetables, and control the water content to be less than 20%.

[0030] Under negative pressure anaerobic conditions, heat up and pyrolyze to generate ash and oil-gas. The oil-gas is sent to the catalytic reaction zone in the upper layer of the pyrolysis reaction fluidized bed, and is further pyrolyzed under the action of the molecular sieve catalyst, and then condensed and recovered to obtain oil liquid. Collect the ash at the bottom of the bed. The reaction pressure of the pyrolysis reaction fluidized bed is -4.2 Mpa, the reaction temperature is 374 °C, the microwave power of the microwave generator is 350 W, the microwave frequency is 600 MHz, the pyrolysis time is 3 h, and the non-condensable gas generated during the condensation of the oil-gas is used for circulation and provides part of the heat for the catalytic pyrolysis reaction fluidized bed.

[0031] S3: Put the oil liquid, hydrogen-supplying mixed solvent, and Ru / C catalyst into a high-pressure reactor for hydrodeoxygenation reaction. The mass ratio of the oil liquid to the hydrogen-supplying mixed solvent is 100:10. The hydrogen-supplying mixed solvent is composed of benzyl alcohol, tetrahydroquinoline, ethyl acetate, and benzyl benzoate in an equal mass ratio. The reaction pressure in the high-pressure reactor is 6 Mpa, the reaction temperature is 350 °C, there is an intermittently opened stirrer in the high-pressure reactor with a stirring rate of 130 r / min, and the reaction time is 1.5 h.

[0032] Subsequently, centrifuge and take the liquid product and place it in an extraction tower. The extractant is pressurized and preheated by a high-pressure pump and then enters the extraction tower for supercritical extraction and upgrading. The extractant is methane, the extraction kettle pressure is 5 Mpa, and the supercritical extraction temperature is 152 °C.

[0033] The material at the top of the extraction tower is transported through a pipeline and enters a first-stage separation tower and a second-stage separation tower under reduced pressure for continuous reduced-pressure separation. The pressure of the first-stage separation tower is 2.1 Mpa and the temperature is 80 °C. The pressure of the second-stage separation tower is 1 Mpa and the temperature is 80 °C. The separated extractant enters the storage tank for extraction circulation. The bottom products of the first-stage separation tower and the second-stage separation tower are respectively sent to a water-oil separator for separation, and the obtained oil-phase mixture is used as the finished product of the biomass liquid fuel. The total acid value of the biomass liquid fuel is 102 mg KOH / g -1 , and the calorific value is 47 MJ / Kg -1 .

[0034] Example 3:

[0035] A method for catalytically cracking biomass to produce liquid fuel, wherein the method is as follows:

[0036] S1: Take 2 Kg of MCM-48 mesoporous molecular sieve and immerse it in an equal mass ratio solution of 1 Kg of cobalt salt and 1 Kg of metal borate in water. After filtration and calcination treatment, a molecular sieve catalyst is obtained. The cobalt salt is cobalt disodium ethylenediaminetetraacetate, and the metal borate is tin borate. The calcination temperature is 440 °C and the calcination time is 3 h;

[0037] S2: Take 80 kg of lignin raw material and 20 kg of sugar raw material, dry them, and put them into a pyrolysis reaction fluidized bed equipped with a microwave generator. The lignin raw material and sugar raw material include wood, rice, sugarcane, and field vegetables, and the water content is controlled to be less than 19%;

[0038] Under negative pressure anaerobic conditions, it is heated and cracked to generate ash and oil gas. The oil gas is sent to the catalytic reaction zone above the pyrolysis reaction fluidized bed, and further cracked under the action of the molecular sieve catalyst, and the oil liquid is condensed and recovered. The ash at the bottom of the bed is collected. The reaction pressure of the pyrolysis reaction fluidized bed is -1.8 Mpa, the reaction temperature is 370 °C, the microwave power of the microwave generator is 600 W, the microwave frequency is 850 MHz, the cracking time is 4 h, and the non-condensable gas generated during the condensation of the oil gas is used for circulation and provides part of the heat for the catalytic cracking reaction fluidized bed;

[0039] S3: Put the oil liquid, hydrogen-supplying mixed solvent, and Ru / C catalyst into a high-pressure reactor for hydrodeoxygenation reaction. The mass ratio of the oil liquid to the hydrogen-supplying mixed solvent is 100:9. The hydrogen-supplying mixed solvent is composed of ethyl acetate and benzyl benzoate in an equal mass ratio. The reaction pressure in the high-pressure reactor is 8 Mpa, the reaction temperature is 295 °C, there is an intermittently opened stirrer with a stirring rate of 110 r / min in the high-pressure reactor, and the reaction time is 2 h;

[0040] Subsequently, centrifuge and take the liquid substance and place it in an extraction tower. The extractant enters the extraction tower for supercritical extraction and upgrading after being pressurized and preheated by a high-pressure pump. The extractant is carbon dioxide or methane, the pressure of the extraction kettle is 5 Mpa, and the supercritical extraction temperature is 130 °C;

[0041] The material at the top of the extraction tower is transported through a pipeline into a first-stage separation tower and a second-stage separation tower for continuous vacuum separation. The pressure of the first-stage separation tower is 2.8 Mpa and the temperature is 90 °C. The pressure of the second-stage separation tower is 2 Mpa and the temperature is 85 °C. The separated extractant enters the storage tank for extraction circulation. The bottom products of the first-stage separation tower and the second-stage separation tower are respectively sent to a water-oil separator for separation, and the obtained single oil phase or oil phase mixture is used as the finished product of biomass liquid fuel. The total acid value of the biomass liquid fuel is 98 mg KOH / g -1 , and the calorific value is 48 MJ / kg -1 .

[0042] Examples 1-3 and commercially available biodiesel (Jinan Jiaxu Chemical Industry) were used as comparative examples, and performance tests were carried out according to the test standards in the table. Example 1a and Example 1b are the biomass liquid fuels of the first-stage separation tower and the second-stage separation tower of the example, respectively. The results are as follows:

[0043]

[0044]

[0045] It can be seen from the above table that the mechanism of the present invention is:

[0046] (1) Using lignin raw materials and sugar raw materials as raw materials and controlling the water content, through catalytic cracking and deoxygenation, C-C bond cleavage and C-H bond cleavage occur. The long carbon chains are cracked into short carbon chains, the sugars are decomposed into oligosaccharides or even monosaccharides or dehydrated anhydride monosaccharide condensates, so that the liquid oil products collected by oil and gas condensation include low-molecular alkanes, unsaturated hydrocarbons, acids, esters, alcohols, ketones, phenols, carbon compounds, furan organic components and related ionic inorganic components. The separated by-product ash can be used to produce solid fuel to improve the by-product income;

[0047] (2) During the cracking process, pyrolysis is carried out by heating up under negative pressure anaerobic conditions, and the non-condensable gas generated during oil and gas condensation is used for circulation and provides part of the heat for the fluidized bed of the catalytic cracking reaction. Microwave-assisted cracking is used to increase the heating rate and make full use of the penetration performance to improve the heat conduction of biomass raw materials with low thermal conductivity. The high-frequency vibration of the microwave magnetic field makes the heating uniform, avoids the phenomenon of external charring and internal uncooked due to temperature difference gradient, and has an obvious catalytic effect on the cracking of macromolecules, which is clean and environmentally friendly, thus improving the energy utilization rate and reducing the thermal energy consumption and loss of cracking;

[0048] (3) During the catalytic cracking process, MCM-48 mesoporous molecular sieve was purchased from Jicang Nano Co., Ltd., which has a uniform pore diameter of about 2.6 nm and two sets of independent three-dimensional helical pore network structures. The CM-48 mesoporous molecular sieve was acid-modified by cobalt salt and metal borate EDTA-2NaCO-Sn / Mo-MCM-48. The two-step method avoids coking deactivation during the catalytic cracking process, prolongs the catalyst activity and life, converts various acids into esters, is conducive to reducing the reaction temperature, increasing the liquid-gas conversion rate and the high-carbon number oil yield, is suitable for the mixture of diesel finished products and lubricating oil semi-finished products, and avoids sulfur pollution;

[0049] (4) Through the hydrogenation and deoxygenation reaction in a high-pressure reactor with a hydrogen supply mixed solvent and a Ru / C catalyst, the oxygen atoms of the oxygen-containing groups in the biomass raw material cracking oil react with hydrogen atoms to break the CO bond and form the CH bond, thereby reducing the acid value and oxygen-containing compound content in the oil, increasing the calorific value of the oil, and effectively inhibiting the formation of visible coke, meeting the requirements of combustion stability and sufficient combustion. The carbon dioxide produced by hydrodeoxygenation can also be used for extraction to reduce costs;

[0050] (5) Using optimized conditions, supercritical extraction is used to improve the quality of the product, and two-stage separation tower vacuum separation is used to separate the product. The water-oil separation is used to extract a single oil phase or an oil phase mixture as the finished biomass liquid fuel. The water generated during the deoxygenation process is reduced, and the product has good solubility and diffusivity, which is beneficial to improving the output value, heat transfer, and inhibiting the polymerization and coking reaction of bio-oil. The extractant methanol can react well with the acids and aldehydes in the bio-oil to produce esters and acetals, thereby reducing the moisture and acid value of the biomass liquid fuel, which is beneficial to improving the calorific value of the product.

[0051] The above is only a preferred specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any changes or substitutions that can be easily thought of by a person skilled in the art within the technical scope disclosed by the present invention should be included in the protection scope of the present invention. Therefore, the protection scope of the present invention should be based on the protection scope of the claims.

Claims

1. A method for catalytically cracking to produce biomass liquid fuel, characterized in that, The method is as follows: S1: Take MCM-48 mesoporous molecular sieve and immerse it in an equimass ratio solution mixed with cobalt salt and metal borate. After filtration and calcination treatment, a molecular sieve catalyst is obtained; S2: Take lignin raw material and sugar raw material, dry them, and put them into a pyrolysis reaction fluidized bed equipped with a microwave generator. Under negative pressure anaerobic conditions, heat up and pyrolyze to generate ash and oil gas. The oil gas is sent to the catalytic reaction zone above the pyrolysis reaction fluidized bed, and further pyrolyzed under the action of the molecular sieve catalyst, and then condensed and recovered to obtain oil liquid, and collect the ash at the bottom of the bed; S3: Take the oil liquid, hydrogen-supplying mixed solvent, and Ru / C catalyst and put them into a high-pressure reactor for hydrodeoxygenation reaction, then centrifuge, take the liquid product and place it in an extraction tower. The extractant is pressurized and preheated by a high-pressure pump and then enters the extraction tower for supercritical extraction and upgrading; S4: The material at the top of the extraction tower is transported through a pipeline into a first-stage separation tower and a second-stage separation tower under reduced pressure for continuous reduced-pressure separation. The separated extractant enters the storage tank for extraction recycling. The bottom products of the first-stage separation tower and the second-stage separation tower are respectively sent to a water-oil separator for separation, and the obtained single oil phase or oil phase mixture is used as the finished product of biomass liquid fuel.

2. A method for catalytic pyrolysis production of biomass liquid fuel according to claim 1, characterized in that, in step S1, the cobalt salt is sodium cobalt ethylenediaminetetraacetate, the metal borate is tin borate or molybdenum borate, the calcination temperature is 350 - 450 °C, and the calcination time is 2 - 3 h.

3. A method for catalytic pyrolysis production of biomass liquid fuel according to claim 1, characterized in that, the lignin raw material includes one or more of wood, bark, wheat, and rice, the sugar raw material includes one or two of sugarcane and field vegetables, and the water content is controlled to be less than 20%.

4. A method for catalytic pyrolysis production of biomass liquid fuel according to claim 1, characterized in that, in step S2, the reaction pressure of the pyrolysis reaction fluidized bed is -5.5 MPa to -0.6 MPa, the reaction temperature is 320 - 385 °C, the microwave power of the microwave generator is 50 - 800 W, the microwave frequency is 500 - 1000 MHz, the pyrolysis time is 3 - 6 h, and the non-condensable gas generated during the condensation of the oil gas is used for circulation and provides part of the heat for the catalytic pyrolysis reaction fluidized bed.

5. A method for catalytic pyrolysis production of biomass liquid fuel according to claim 1, characterized in that, in step S3, the mass ratio of the oil liquid to the hydrogen-supplying mixed solvent is 100:(6 - 15), and the hydrogen-supplying mixed solvent is composed of two or more of benzyl alcohol, tetrahydroquinoline, tetrahydrophenanthrene, ethyl acetate, and benzyl benzoate in an equimass ratio.

6. A method for catalytic pyrolysis production of biomass liquid fuel according to claim 1, characterized in that, in step S3, the reaction pressure in the high-pressure reactor is 5-8 MPa, the reaction temperature is 280-370 °C, a stirrer with intermittent opening and a stirring rate of 80-150 r / min is provided in the high-pressure reactor, and the reaction time is 1-2 h.

7. A method for catalytic pyrolysis production of biomass liquid fuel according to claim 1, characterized in that, the extractant in step S3 is carbon dioxide or methane, the pressure of the extraction kettle is 4-6 MPa, the supercritical access temperature is 100-155 °C, in step S4, the pressure of the first separation tower is 2.1-3 MPa and the temperature is 70-110 °C, and the pressure of the second separation tower is 1-2 MPa and the temperature is 65-100 °C.

8. A method for catalytically cracking to produce biomass liquid fuel according to any one of claims 1-7, characterized in that, The total acid value of the biomass liquid fuel is 80 mgKOH / g - 135 mgKOH / g, and the calorific value is 38 MJ / kg - 51 MJ / kg.

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