Method for preparing traffic fuel oil by utilizing hydrothermal liquefied biological crude oil

Abstract

The invention relates to the technical field of treatment of biological crude oil, in particular to a method for preparing traffic fuel oil from hydrothermal liquefied biological crude oil. The method comprises the following steps: carrying out distillation treatment on hydrothermal liquefied biological crude oil to obtain purified biological oil and distillation residues; carrying out hydrocracking reaction on the purified bio-oil to obtain cracked bio-oil; performing catalytic hydrogenation reaction on the cracked bio-oil to obtain refined bio-oil; and fractionating the refined bio-oil to obtain the traffic fuel oil. By means of the method, conversion from hydrothermal liquefaction of biological crude oil to traffic fuel oil which can be applied to diesel oil, gasoline and aero-engines is achieved. Distillation residues generated in the distillation process are subjected to metal recovery to prepare high-quality biochar for subsequent field returning. The hydrogen used in the hydrogenation process can come from hydrothermal liquefaction wastewater treatment, so that full recycling and energy regeneration of raw materials are realized.

Description

Technical Field

[0001] The invention relates to the technical field of bio-crude oil processing, and in particular to a method for preparing traffic fuel by hydrothermal liquefaction of bio-crude oil. Background Art

[0002] With the continuous exploitation of resources, the reserves of traditional fossil energy (coal, oil, natural gas, etc.) are gradually decreasing, and the pressure on energy supply is increasing. In this context, biocrude oil, as a renewable energy fuel, has gradually attracted widespread attention. Compared with traditional fossil fuels, biocrude oil has the advantages of being renewable and producing fewer combustion pollutants, which is of great significance for solving energy crises and environmental pollution problems. It is worth noting that compared with conventional fuel oil, biocrude oil has problems such as low carbon and hydrogen content, high oxygen content, and low calorific value, and cannot provide sufficient power. At the same time, factors such as high acidity and high viscosity also restrict the use of biocrude oil. Therefore, optimizing and improving the preparation process and performing subsequent treatments such as hydrogenation and upgrading of biocrude oil to improve the stability of biocrude oil and improve related parameters have become current research hotspots.

[0003] At present, bio-crude oil is prepared mainly by two methods: pyrolysis and hydrothermal liquefaction. Pyrolysis refers to the process of converting biomass into bio-crude oil, charcoal and gas products through thermal decomposition reaction under the condition of isolating air or supplying a small amount of air. At present, the fuel conversion of bio-crude oil mostly uses pyrolysis bio-crude oil, and adopts processes such as hydrorefining and catalytic reforming to obtain a single transportation fuel (diesel, gasoline, aviation kerosene, etc.) that can be partially replaced / directly applied. It has high requirements for the type of biomass raw materials, processing technology, reaction conditions, application scenarios, etc., which is not conducive to the promotion of bio-crude oil fuel conversion technology. In comparison, the hydrothermal liquefaction method realizes the thermochemical conversion of biomass to obtain bio-crude oil under high temperature and high pressure water phase conditions, and does not require the drying of biomass, so the types of biomass raw materials that can be selected are wider. In addition, compared with pyrolysis bio-crude oil, hydrothermal liquefaction bio-crude oil has the advantages of low water content, low oxygen content, and high calorific value, and is more suitable for quality improvement to achieve fuel conversion. Therefore, how to provide a hydrothermal liquefaction bio-crude oil fuel conversion technology has become a technical problem to be solved in this field. Summary of the invention

[0004] The purpose of the present invention is to provide a method for preparing traffic fuel by utilizing hydrothermal liquefaction of bio-crude oil, thereby realizing the conversion of hydrothermal liquefaction of bio-crude oil into traffic fuel applicable to diesel engines, gasoline engines and aviation engines, and the distillation residue obtained by distillation treatment can be used to prepare high-quality biochar after metal recovery for subsequent return to the field, thereby realizing full resource and energy utilization of raw materials.

[0005] In order to achieve the above-mentioned object of the invention, the present invention provides the following technical solutions:

[0006] The present invention provides a method for preparing traffic fuel by hydrothermal liquefaction of bio-crude oil, comprising the following steps:

[0007] 1) distilling the hydrothermal liquefied bio-crude oil to obtain purified bio-oil and distillation residue;

[0008] 2) performing a hydrocracking reaction on the purified bio-oil to obtain cracked bio-oil;

[0009] 3) subjecting the cracked bio-oil to a catalytic hydrogenation reaction to obtain refined bio-oil;

[0010] 4) fractionating the refined bio-oil to obtain traffic fuel.

[0011] Optionally, the distillation treatment temperature is 150-350°C.

[0012] Optionally, the temperature of the hydrocracking reaction is 300-550° C., the time is 0.5-6 h, the hydrogen pressure is 5-20 MPa, and the hydrogen-to-oil ratio is 0.005-0.03.

[0013] Optionally, the hydrocracking reaction is carried out in the presence of a hydrocracking catalyst, wherein the hydrocracking catalyst is a bifunctional catalyst, and the bifunctional catalyst is composed of a metal hydrogenation component and an acidic support;

[0014] The metal hydrogenation component comprises at least one of the following components: oxides of metal elements in Group VIB and Group VIII, sulfides of metal elements in Group VIB and Group VIII, and noble metals;

[0015] The acidic support comprises at least one of the following components: aluminosilicate ore, artificial zeolite and molecular sieve.

[0016] Optionally, the hydrocracking catalyst is pre-sulfurized before use; the mass ratio of the purified bio-oil to the hydrocracking catalyst is 1.6 to 20:1.

[0017] Optionally, the temperature of the catalytic hydrogenation reaction is 200-400° C., the time is 1-6 hours, the hydrogen pressure is 2-10 MPa, and the hydrogen-to-oil ratio is 0.01-0.04.

[0018] Optionally, the catalytic hydrogenation reaction is carried out in the presence of a hydrogenation catalyst, and the hydrogenation catalyst includes at least one of the following components: NiMo / Al2O3 catalyst and Pt / Al2O3 catalyst.

[0019] Optionally, the mass ratio of the cracked bio-oil to the hydrogenation catalyst is 2:1.

[0020] Optionally, the traffic fuel includes gasoline, aviation kerosene and diesel; when the distillation temperature is 30-150°C, the collected fraction is gasoline; when the distillation temperature is 150-250°C, the collected fraction is aviation kerosene; when the distillation temperature is 250-350°C, the collected fraction is diesel.

[0021] Optionally, the method further comprises recovering metals from the distillation residue and then preparing biochar.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] 1. The present invention realizes the conversion of hydrothermal liquefied bio-crude oil into traffic fuel applicable to diesel engines, gasoline engines and aviation engines through a process combining distillation purification, hydrocracking, catalytic hydrogenation and product fractionation.

[0024] 2. The present invention preliminarily purifies the hydrothermal liquefied bio-crude oil by distillation, removes impurities such as metals, salts, and micro carbon particles in the bio-crude oil, and avoids problems such as catalyst metal poisoning and difficulty in removing solid impurities in the subsequent treatment process. The distillation residue obtained in the distillation process can be used for metal recovery and then to prepare biochar for biological return to the field, thereby realizing resource utilization of raw materials.

[0025] 3. The present invention converts the heavy oil in the bio-oil into light oil by subjecting the purified bio-oil to hydrocracking treatment, and combines it with subsequent catalytic hydrogenation treatment to further remove harmful substances such as sulfur, oxygen, nitrogen, etc. in the bio-oil, thereby improving the quality of the bio-oil, and finally obtaining transportation fuel products that can be directly used in diesel, gasoline and aviation engines through distillation.

[0026] 4. The hydrogen used in the hydrogenation process of the present invention can be directly derived from hydrothermal liquefaction wastewater treatment, and can also be obtained by combining dark fermentation of biomass waste to produce hydrogen, microbial electrochemical hydrogen production and other processes, thereby achieving full utilization of front-end hydrothermal liquefaction wastewater and biomass waste.

[0027] 5. The present invention breaks through the limitations of the prior art on the types of biomass raw materials for preparing hydrothermal liquefaction of bio-crude oil, the application scenarios of upgraded bio-oil, etc., and provides a feasible technical solution for the application and promotion of the technical route of biomass hydrothermal liquefaction-bio-crude oil fuel conversion. DETAILED DESCRIPTION

[0028] Various exemplary embodiments of the present invention will now be described in detail. This detailed description should not be considered as limiting the present invention, but should be understood as a more detailed description of certain aspects, features, and embodiments of the present invention.

[0029] It should be understood that the terms described in the present invention are only for describing special embodiments and are not intended to limit the present invention. In addition, for the numerical range in the present invention, it should be understood that each intermediate value between the upper and lower limits of the scope is also specifically disclosed. Each smaller range between the intermediate value in any stated value or stated range and any other stated value or intermediate value in the described range is also included in the present invention. The upper and lower limits of these smaller ranges can be independently included or excluded in the scope.

[0030] Unless otherwise indicated, all technical and scientific terms used herein have the same meanings as those generally understood by those skilled in the art. Although the present invention describes only preferred methods and materials, any methods and materials similar or equivalent to those described herein may also be used in the implementation or testing of the present invention. All documents mentioned in this specification are incorporated by reference to disclose and describe the methods and / or materials associated with the documents. In the event of a conflict with any incorporated document, the content of this specification shall prevail.

[0031] It will be apparent to those skilled in the art that various modifications and variations may be made to the specific embodiments of the present invention description without departing from the scope or spirit of the present invention. Other embodiments derived from the present invention description will be apparent to those skilled in the art. The present application description and examples are exemplary only.

[0032] The words “include,” “including,” “have,” “contain,” etc. used in this document are open-ended terms, meaning including but not limited to.

[0033] The raw materials used in the present invention can be obtained from the market or prepared by the existing technology.

[0034] The present invention provides a method for preparing traffic fuel by hydrothermal liquefaction of bio-crude oil, comprising the following steps:

[0035] 1) distilling the hydrothermal liquefied bio-crude oil to obtain purified bio-oil and distillation residue;

[0036] 2) performing a hydrocracking reaction on the purified bio-oil to obtain cracked bio-oil;

[0037] 3) subjecting the cracked bio-oil to a catalytic hydrogenation reaction to obtain refined bio-oil;

[0038] 4) fractionating the refined bio-oil to obtain traffic fuel.

[0039] The present invention firstly performs distillation treatment on hydrothermal liquefied bio-crude oil to obtain purified bio-oil and distillation residue.

[0040] The present invention has no particular limitation on the source of the hydrothermal liquefied bio-crude oil, which can be prepared from any biomass and hydrothermal liquefaction method. In an embodiment of the present invention, the preparation method of the hydrothermal liquefied bio-crude oil is as follows: after the biomass raw material is mixed with water, a hydrothermal liquefaction treatment is performed to obtain a liquid phase, a gas phase and algae residue, and the liquid phase product is separated to obtain a water phase and bio-crude oil.

[0041] The biomass raw material is spirulina dry powder, sewage sludge or kitchen waste; the usage ratio of the biomass raw material to water is 1g:6mL; the temperature of the hydrothermal liquefaction treatment is 300°C and the time is 30min.

[0042] In the present invention, the distillation process can be a common distillation method such as atmospheric distillation or reduced pressure distillation. In an embodiment of the present invention, the distillation process is carried out under normal pressure (i.e., standard atmospheric pressure).

[0043] In some embodiments of the present invention, the temperature of the distillation treatment is 150-350°C, preferably 160-300°C, more preferably 180-250°C, and even more preferably 200-220°C.

[0044] In the present invention, the time of the distillation process is not limited and may vary according to different raw materials. The distillation process may be stopped when no more liquid flows out. In the embodiment of the present invention, the distillation process is terminated when no more liquid is collected in the vacuum receiver of the distillation device.

[0045] In the present invention, the method further comprises recovering metals from the distillation residue, and then preparing biochar for biological return to the field. In the present invention, the metal recovery method is a conventional recovery method in the art, and the preparation method of the biochar includes but is not limited to pyrolysis, roasting, etc.; the biochar can be returned to the field to improve the soil, or used as a catalyst.

[0046] After obtaining the purified bio-oil, the present invention performs a hydrocracking reaction on the purified bio-oil to obtain cracked bio-oil.

[0047] In some embodiments of the present invention, the temperature of the hydrocracking reaction is 300-550°C, preferably 320-500°C, more preferably 350-450°C, and further preferably 400-420°C; the time is 0.5-6h, more preferably 2-5h, and further preferably 3-4h; the hydrogen pressure is 5-20MPa, preferably 8-16MPa, and further preferably 10-12MPa; the hydrogen-to-oil ratio is 0.005-0.03, preferably 0.01-0.02, and further preferably 0.015.

[0048] In some embodiments of the present invention, the hydrocracking reaction is carried out in the presence of a hydrocracking catalyst, and the hydrocracking catalyst is a bifunctional catalyst; the bifunctional catalyst consists of a metal hydrogenation component and an acidic support.

[0049] In some embodiments of the present invention, the metal hydrogenation component includes at least one of the following components: oxides of metal elements in Group VIB and Group VIII, sulfides of metal elements in Group VIB and Group VIII, and noble metals;

[0050] The metal elements in Group VIB and Group VIII include Fe, Co, Ni, Cr, Mo, W, etc., preferably W and Ni;

[0051] The acidic support comprises at least one of the following components: aluminosilicate ore, artificial zeolite, amorphous silica-alumina and molecular sieve, preferably amorphous silica-alumina.

[0052] In an embodiment of the present invention, the hydrocracking catalyst is a FC-14 catalyst.

[0053] In some embodiments of the present invention, the hydrocracking catalyst is presulfurized before use to improve the catalytic effect of the catalyst. In an embodiment of the present invention, the hydrocracking catalyst is treated by a dry presulfurization method. Specifically, the hydrocracking catalyst is mixed with dimethyl sulfide in the presence of a hydrogen-nitrogen mixed gas and reacted at 150 to 350° C. When the concentration of hydrogen sulfide in the circulating gas no longer changes, the presulfurization treatment is completed; wherein the mass ratio of the hydrocracking catalyst to dimethyl sulfide is 2:1.

[0054] In some embodiments of the present invention, the mass ratio of the purified bio-oil to the hydrocracking catalyst is 1.6 to 20:1, preferably 2 to 5:1.

[0055] In some embodiments of the present invention, the purified bio-oil and the hydrocracking catalyst are preferably stirred after mixing, so that the materials are evenly mixed during the hydrocracking reaction. The present invention has no special requirements for the stirring, as long as the purified bio-oil and the hydrocracking catalyst can be evenly mixed.

[0056] In the present invention, the hydrocracking reaction is carried out in an environment filled with hydrogen. In an embodiment of the present invention, nitrogen is first blown before the hydrocracking reaction to ensure an oxygen-free environment. After the nitrogen blow is completed, hydrogen is blown to remove the residual nitrogen in the reactor so that the reactor is only filled with hydrogen.

[0057] In some embodiments of the present invention, after the hydrocracking reaction is completed, the reaction product is post-processed to obtain cracked bio-oil; the post-processing preferably includes the following steps: cooling the reaction product, filtering to obtain a liquid phase product, separating the liquid phase product into phases to obtain an oil phase, i.e., cracked bio-oil. In some embodiments of the present invention, the cooling method is preferably to cool the reaction product by cooling the reactor with water; the filtration is preferably performed through a metal mesh to separate the hydrocracking catalyst; the present invention has no special requirements for the phase separation method, as long as the water phase and the oil phase can be separated. In the embodiment of the present invention, the phase separation is performed by centrifugation; the centrifugal speed is preferably 3000-5000rpm, preferably 4000rpm; the time is 3-8min, preferably 5min.

[0058] In an embodiment of the present invention, in order to improve the yield, acetone is used to clean the inside of the reactor, the metal mesh and the hydrocracking catalyst to obtain a cleaning liquid, and then the cleaning liquid is distilled to remove the acetone, and the obtained substrate is recovered and combined with the cracked bio-oil for the next step of processing; in an embodiment of the present invention, the cleaning liquid is distilled using a rotary evaporator.

[0059] After obtaining the cracked bio-oil, the present invention performs catalytic hydrogenation reaction on the cracked bio-oil to obtain refined bio-oil.

[0060] In some embodiments of the present invention, the temperature of the catalytic hydrogenation reaction is 200-400°C, preferably 250-380°C, more preferably 280-360°C, and more preferably 300-350°C; the time is 1-6h, preferably 2-5h, and more preferably 3-4h; the hydrogen pressure is 2-10MPa, preferably 3-6MPa, and more preferably 4-5MPa; the hydrogen-to-oil ratio is 0.01-0.04, and more preferably 0.02-0.03.

[0061] In some embodiments of the present invention, the catalytic hydrogenation reaction is carried out in the presence of a hydrogenation catalyst;

[0062] The hydrogenation catalyst comprises at least one of the following components: NiMo / Al2O3 catalyst and Pt / Al2O3 catalyst, preferably NiMo / Al2O3 catalyst.

[0063] In some embodiments of the present invention, when the above hydrogenation catalyst is used, the hydrogenation catalyst is pre-sulfurized before use to improve the catalytic effect of the catalyst. In an embodiment of the present invention, the hydrogenation catalyst is treated by a dry pre-sulfurization method. Specifically, the hydrogenation catalyst is mixed with dimethyl sulfide in the presence of a hydrogen-nitrogen mixed gas and reacted at 150 to 350° C. When the concentration of hydrogen sulfide in the circulating gas no longer changes, the pre-sulfurization treatment is completed; wherein the mass ratio of the hydrogenation catalyst to dimethyl sulfide is 2:1.

[0064] The mass ratio of the cracked bio-oil to the hydrogenation catalyst is 2:1.

[0065] In the present invention, the catalytic hydrogenation reaction is carried out in an environment filled with hydrogen. In an embodiment of the present invention, nitrogen is first blown before the hydrocracking reaction to ensure an oxygen-free environment. After the nitrogen blow is completed, hydrogen is blown to remove the residual nitrogen in the reactor so that the reactor is only filled with hydrogen.

[0066] In some embodiments of the present invention, after the catalytic hydrogenation reaction is completed, the reaction product is post-treated to obtain refined bio-oil; the post-treatment of the reaction product of the catalytic hydrogenation reaction is preferably the same as the post-treatment method of the reaction product of the hydrocracking reaction, which will not be repeated here.

[0067] After obtaining the refined bio-oil, the present invention fractionates the refined bio-oil to obtain traffic fuel.

[0068] In some embodiments of the present invention, the transportation fuel includes gasoline, aviation kerosene and diesel.

[0069] In some embodiments of the present invention, when the distillation temperature is 30-150°C, the collected fraction is gasoline; when the distillation temperature is 150-250°C, the collected fraction is aviation kerosene; when the distillation temperature is 250-350°C, the collected fraction is diesel.

[0070] The technical solutions provided by the present invention are described in detail below in conjunction with the embodiments, but they should not be construed as limiting the protection scope of the present invention.

[0071] Example 1

[0072] 1) 2 g of spirulina powder was selected as the biomass raw material, 12 ml of water was added, and hydrothermal liquefaction was carried out at 300° C. The reaction time was 30 min to obtain a liquid phase, a gas phase and algae residue, and the liquid phase product was separated to obtain an aqueous phase and bio-crude oil.

[0073] 2) The bio-crude oil obtained in step 1) is subjected to atmospheric distillation at 200° C. When no more liquid flows out of the vacuum receiver of the distillation device, the distillation process is terminated to obtain purified bio-oil and distillation residue. The distillation residue is subjected to metal recovery and then pyrolyzed to prepare biochar.

[0074] 3) 4 g of FC-14 hydrocracking catalyst and 2 g of dimethyl sulfide are mixed, and the reaction temperature is controlled at 150-350° C. in the presence of a hydrogen-nitrogen mixed gas. When the concentration of hydrogen sulfide in the circulating gas no longer changes, the presulfidation treatment is completed to obtain a presulfided FC-14 hydrocracking catalyst;

[0075] 6g of NiMo / Al2O3 catalyst and 3g of dimethyl sulfide are mixed, and the reaction temperature is controlled at 150-350°C in the presence of a hydrogen-nitrogen mixed gas. When the concentration of hydrogen sulfide in the circulating gas no longer changes, the presulfurization treatment is completed to obtain a presulfurized NiMo / Al2O3 catalyst.

[0076] 4) Add 4 g of purified bio-oil and 2 g of presulfurized FC-14 hydrocracking catalyst to a 25 mL reactor, and perform repeated nitrogen purging to ensure an oxygen-free environment in the reactor. After the nitrogen purging is completed, hydrogen purging is used to remove the residual nitrogen in the reactor and the hydrogen is pressurized to an initial pressure of 10 MPa. Stirring is turned on, the temperature of the reactor is set to 400°C, and the temperature is kept for 4 hours. The weight hourly space velocity (WHSV) of the reaction process is 0.5 g / gcat h, and the hydrogen-to-oil ratio is 0.015. After the reaction is completed, the reactor is cooled with water, and the reaction product is filtered through a metal mesh to remove the FC-14 hydrocracking catalyst to obtain a liquid product. The liquid product is centrifuged at a speed of 4000 rpm for 5 minutes to separate the oil phase and the water phase, and the oil phase is collected and recorded as bio-oil 1. The inside of the reactor, the metal mesh and the FC-14 hydrocracking catalyst are cleaned with 100 mL of acetone, and the acetone is removed from the cleaning liquid using a rotary evaporator to obtain bio-oil 2. Bio-oil 1 and bio-oil 2 were combined to obtain cracked bio-oil.

[0077] 5) Add 6g of cracked bio-oil and 3g of presulfurized NiMo / Al2O3 catalyst to another 25mL reactor, first use nitrogen to purge the reactor to ensure an oxygen-free environment, then use hydrogen to purge to remove residual nitrogen, and pressurize the hydrogen to an initial pressure of 4MPa. Set the temperature of the reactor to 350°C and keep it warm for 4h. The weight hourly space velocity of the reaction process is also 0.5g / gcath, and the hydrogen-to-oil ratio is 0.02. After the reaction is completed, the same post-treatment method as step 4) is used to obtain refined bio-oil.

[0078] 6) The refined bio-oil obtained in step 5) is heated and fractionated, and the fraction at 30-150° C. is collected to obtain 20% gasoline, and the temperature is further increased to collect the fraction at 150-250° C. to obtain 45% aviation kerosene, and finally the temperature is increased again to collect the fraction above 250-350° C. to obtain 35% diesel.

[0079] The elemental composition, hydrogen-carbon atomic ratio (H / C), and higher heating value (HHV) of the products (hydrothermal liquefied bio-crude oil (A), purified bio-oil (B), cracked bio-oil (C), and refined bio-oil (D)) obtained in step 1), step 2), step 4), and step 5) were analyzed, and the results are shown in Table 1-1.

[0080] Table 1-1 Related parameters of the obtained bio-oil

[0081] Product Categories C (wt%) H (wt%) O(wt%) N (wt%) H / C HHV(MJ / kg) A 75.0±0.3 10.6±0.1 6.9±0.3 7.5±0.1 1.66±0.02 37.9±0.2 B 79.3±0.3 11.1±0.1 3.9±0.3 5.7±0.1 1.68±0.02 40.3±0.2 C 82.7±0.4 11.7±0.2 1.4±0.5 4.2±0.2 1.69±0.01 42.5±0.2 D 85.6±0.2 12.3±0.2 0.2±0.4 1.9±0.1 1.72±0.02 44.3±0.3

[0082] It can be seen from Table 1-1 that the process has an excellent quality improvement effect on hydrothermal liquefaction of bio-crude oil.

[0083] The diesel, aviation kerosene and gasoline obtained in step 5) were tested according to the test methods in the technical requirements for National VI0 for automotive diesel (GB1914-2016), the technical requirements for No. 3 jet fuel (aviation kerosene, GB 6537-2018), and the technical requirements for VIA92 for automotive gasoline (GB 17930-2016), respectively. The results are shown in Tables 1-2, 1-3, and 1-4.

[0084] Table 1-2 Comparative analysis of diesel properties

[0085]

[0086]

[0087] Table 1-3 Comparative analysis of the properties of the obtained aviation kerosene

[0088]

[0089]

[0090]

[0091] Table 1-4 Comparative analysis of the properties of the obtained gasoline

[0092]

[0093]

[0094] The test results show that the transportation fuel produced through this process meets the relevant national standards and has excellent results.

[0095] Example 2

[0096] The only difference from Example 1 is that the material used to prepare the hydrothermal liquefied bio-crude oil is sewage sludge.

[0097] Correspondingly, the bio-oil related parameters obtained during the experiment were measured, and the results are shown in Table 2-1.

[0098] Table 2-1 Related parameters of the obtained bio-oil

[0099]

[0100]

[0101] It can be seen from Table 2-1 that for hydrothermal liquefied bio-crude oil with a high oxygen content, this method still has an excellent quality improvement effect and achieves effective removal of impurities.

[0102] The key parameters of the prepared traffic fuel were measured using the same evaluation criteria as in Example 1. The results are shown in Tables 2-2, 2-3, and 2-4.

[0103] Table 2-2 Comparative analysis of diesel properties

[0104]

[0105] Table 2-3 Comparative analysis of the properties of the obtained aviation kerosene

[0106]

[0107]

[0108] Table 2-4 Comparative analysis of gasoline properties

[0109]

[0110]

[0111] The test results show that the transportation fuel produced through this process meets the relevant national standards and has excellent results.

[0112] Example 3

[0113] The only difference from Example 1 is that the material for preparing the hydrothermal liquefied bio-crude oil is food waste.

[0114] Correspondingly, the bio-oil related parameters obtained during the experiment were measured, and the results are shown in Table 3-1.

[0115] Table 3-1 Related parameters of the obtained bio-oil

[0116] Product Categories C (wt%) H (wt%) O(wt%) N (wt%) H / C HHV(MJ / kg) A 76.6±0.1 11.0±0.1 11.8±0.1 0.6±0.0 1.72±0.02 38.7±0.1 B 81.9±0.2 13.1±0.2 4.5±0.1 0.5±0.0 1.92±0.01 43.7±0.1 C 84.8±0.2 13.7±0.1 1.2±0.1 0.3±0.0 1.94±0.02 45.8±0.2 D 85.9±0.2 14.1±0.2 0.0±0.0 0.0±0.1 1.97±0.01 46.8±0.1

[0117] It can be seen from Table 3-1 that for raw materials with relatively high initial hydrogen and carbon content, such as hydrothermal liquefaction of food waste bio-crude oil, this process still has a good improvement effect.

[0118] The key parameters of the prepared traffic fuel were measured using the same evaluation criteria as in Example 1. The results are shown in Tables 3-2, 3-3, and 3-4.

[0119] Table 3-2 Comparative analysis of diesel properties

[0120]

[0121]

[0122] Table 3-3 Comparative analysis of the properties of the obtained aviation kerosene

[0123]

[0124]

[0125] Table 3-4 Comparative analysis of gasoline properties

[0126]

[0127]

[0128] The test results show that the transportation fuel produced through this process meets the relevant national standards and has excellent results.

[0129] The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principle of the present invention. These improvements and modifications should also be regarded as the scope of protection of the present invention.

Claims

1. A method for preparing traffic fuel by hydrothermal liquefaction of bio-crude oil, characterized in that: The following steps are involved: 1) distilling the hydrothermal liquefied bio-crude oil to obtain purified bio-oil and distillation residue; 2) performing a hydrocracking reaction on the purified bio-oil to obtain cracked bio-oil; 3) subjecting the cracked bio-oil to a catalytic hydrogenation reaction to obtain refined bio-oil; 4) fractionating the refined bio-oil to obtain traffic fuel.

2. The method according to claim 1, characterized in that The temperature of the distillation treatment is 150-350°C.

3. The method according to claim 1, characterized in that: The temperature of the hydrocracking reaction is 300-550° C., the time is 0.5-6 hours, the hydrogen pressure is 5-20 MPa, and the hydrogen-to-oil ratio is 0.005-0.

03.

4. The method according to claim 3, characterized in that The hydrocracking reaction is carried out in the presence of a hydrocracking catalyst, wherein the hydrocracking catalyst is a bifunctional catalyst, and the bifunctional catalyst is composed of a metal hydrogenation component and an acidic support; The metal hydrogenation component comprises at least one of the following components: oxides of metal elements in Group VIB and Group VIII, sulfides of metal elements in Group VIB and Group VIII, and noble metals; The acidic support comprises at least one of the following components: aluminosilicate ore, artificial zeolite and molecular sieve.

5. The method according to claim 3 or 4, characterized in that: The hydrocracking catalyst is pre-sulfurized before use; the mass ratio of the purified bio-oil to the hydrocracking catalyst is 1.6-20:

1.

6. The method according to claim 1, characterized in that The temperature of the catalytic hydrogenation reaction is 200-400° C., the time is 1-6 hours, the hydrogen pressure is 2-10 MPa, and the hydrogen-to-oil ratio is 0.01-0.

04.

7. The method according to claim 6, characterized in that The catalytic hydrogenation reaction is carried out in the presence of a hydrogenation catalyst, and the hydrogenation catalyst includes at least one of the following components: a NiMo / Al2O3 catalyst and a Pt / Al2O3 catalyst.

8. The method according to claim 6 or 7, characterized in that: The mass ratio of the cracked bio-oil to the hydrogenation catalyst is 2:

1.

9. The method according to claim 1, characterized in that: The traffic fuel includes gasoline, aviation kerosene and diesel; when the distillation temperature is 30-150°C, the collected fraction is gasoline; when the distillation temperature is 150-250°C, the collected fraction is aviation kerosene; when the distillation temperature is 250-350°C, the collected fraction is diesel.

10. The method according to claim 1, characterized in that The method further comprises recovering metals from the distillation residue and then preparing biochar.

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