Application of boehmite catalyst in processing and treating fossil energy sources, material for processing and treating fossil energy sources and method for processing and treating fossil energy sources

Abstract

The invention relates to the technical field of fossil energy sources and mining, in particular to application of a boehmite catalyst in processing and treating the fossil energy sources, a material for processing and treating the fossil energy sources and a method for processing and treating the fossil energy sources. A method of processing and treating fossil-based energy by two stages; the invention also discloses an application of the thermochemical conversion reaction product prepared by the method. The boehmite catalyst is used for thermochemical conversion of fossil energy (especially oil shale), activation energy of the thermochemical conversion of the fossil energy (especially oil shale) can be obviously reduced, and the product can be upgraded and modified through the thermochemical conversion of the fossil energy (especially oil shale). The resulting thermochemical conversion reaction product can be used to produce high quality petroleum-like fuels or valuable chemicals.

Description

Technical Field

[0001] The present invention relates to the field of fossil energy and mining technology, and in particular to an application of a boehmite catalyst in processing and treating fossil energy, a material for processing and treating fossil energy, a method for processing and treating fossil energy, a method for processing and treating fossil energy through two stages, and an application of a thermochemical conversion reaction product obtained by the method. Background Art

[0002] With the growth of population, the rapid development of urbanization, industrialization and globalization, conventional fossil energy such as natural gas, crude oil and coal is becoming increasingly depleted. The energy crisis caused by this has become one of the important bottlenecks restricting the sustainable and healthy development of the economy and society. At present, there are probably two ways to solve these problems. The first way is to use new green renewable energy such as solar energy, wind energy, geothermal energy to replace conventional fossil energy. These renewable energy sources are usually green and sustainable, and they are also in line with the overall goals and trends of carbon peak and carbon neutrality at home and abroad. This is an energy that is hailed as likely to make an important contribution to this field in the future. However, at the same time, we should also note that although this type of energy is highly sought after, at present, the consumption of new green renewable energy accounts for less than 20% of global energy consumption, while the consumption of fossil energy accounts for more than 80%. This is because there are still some problems with the new green renewable energy. First of all, its technology is not yet mature, and the technical bottleneck makes it impossible to completely replace fossil energy at present. In addition, the new green renewable energy does not have material properties. In addition to its energy attributes, fossil energy also has material attributes and plays an important role in the fields of materials, food, and drug synthesis. This is irreplaceable by new green renewable energy sources. For example, it is currently difficult for us to obtain ethylene from wind energy, which can be further polymerized to produce polyethylene, and then further produced into plastics. In order to cope with the energy crisis, in addition to the research and development and utilization of new green renewable energy sources, there is another way, which is to develop and utilize unconventional fossil energy represented by oil shale, heavy oil, oil sands, etc., which has abundant reserves and is widely distributed. This has become an important solution that the industry generally pays attention to.

[0003] Among various unconventional fossil energy sources, oil shale is widely distributed and has large reserves. Its proven reserves in the strata are equivalent to 689 billion tons of shale oil, which is about 4 times the world's recoverable crude oil reserves (about 170 billion tons). At present, my country's proven oil shale resources are 719.9 billion tons, equivalent to 47.6 billion tons of shale oil, ranking second in the world. If these oil shales are mined, it can largely solve the energy dilemma of my country and even the world.

[0004] In simple terms, oil shale is mainly a sedimentary rock with an inorganic mineral skeleton and rich in solid combustible organic matter (kerogen). Its kerogen organic matter is the main oil-forming material precursor of oil shale, and its ideal hydrogen-carbon atomic ratio is conducive to its fuelization through various means. Thermochemical conversion treatment is one of the most common treatment methods for oil shale, and thermochemical conversion treatment can convert oil shale into small molecules. However, oil shale has a complex structure and contains a large number of heteroatoms and inorganic minerals. Therefore, the oil produced by the thermochemical conversion of oil shale is of poor quality and difficult to use directly. In addition, the energy consumption of the thermochemical conversion reaction of oil shale is very high, and at present, from the perspective of literature, there is little research on the production of high value-added chemicals using the material properties of oil shale. This leads to high energy consumption in the thermochemical conversion process of oil shale, poor oil quality (many heteroatoms), and insufficient use of material properties.

[0005] In recent years, researchers at home and abroad have used various types of catalysts to study their different catalytic properties for thermochemical conversion reactions of oil shale. These catalysts mainly include natural minerals (mainly including carbonate minerals, silicate minerals, calcite, dolomite, kaolinite, gypsum, montmorillonite, pyrite, illite, shale ash, etc.), inorganic metal salts (mainly including FeCl2, FeCl3, CoCl2, NiCl2, ZnCl2, SnCl2, MnSO4 and MoS2, etc.), organic metal salts (for example, CH3COONa and (CH3COO)2Ca, etc.), metal oxides or carbonyl compounds (mainly including MgO, Fe2O3, MoO3, Mo(CO)6, and Cr(CO)6, etc.), molecular sieves (mainly including X-type, A-type, ZSM~5 and SBA molecular sieves, etc.), polymers (for example, polypropylene, etc.), and loaded or modified materials (for example, loading one or more active ingredients such as Zn, Ni, Cu and Mo on natural minerals and molecular sieves, or modifying natural minerals and molecular sieves, etc.), etc. However, these catalysts still have many problems. For example, they are difficult to mass produce, have poor stability, high preparation costs, complex processes, require various hazardous or expensive raw materials or precursors, are easily deactivated due to pore blockage, have poor selectivity, require long impregnation and subsequent drying processes, or require tedious pretreatment of oil shale. These problems limit the large-scale application of these catalysts.

[0006] Therefore, how to effectively reduce activation energy / energy consumption; improve thermochemical conversion rate and increase oil and gas yield; improve the quality of oil and gas products, such as removing impurities; produce high value-added chemical products and further develop their material properties, etc., are still important topics worthy of study. Summary of the invention

[0007] The purpose of the present invention is to overcome the problems of expensiveness, poor stability, complicated use and poor catalytic activity of catalysts currently used in thermochemical conversion reactions of fossil energy. The present invention specifically relates to an application of a boehmite catalyst in processing and treating fossil energy, a material for processing and treating fossil energy, a method for processing and treating fossil energy; a method for processing and treating fossil energy in two stages; and an application of a thermochemical conversion reaction product obtained by the method.

[0008] The boehmite catalyst studied in the present invention is used for the thermochemical conversion of fossil energy (especially oil shale), which can significantly reduce the activation energy of the thermochemical conversion of fossil energy (especially oil shale), and can also improve the quality of the products through the thermochemical conversion of fossil energy (especially oil shale). The obtained thermochemical conversion reaction products can be used to produce high-quality petroleum-like fuels or precious chemicals.

[0009] In order to achieve the above-mentioned object, the first aspect of the present invention provides a boehmite catalyst for use in processing and treating fossil energy; the chemical formula of the boehmite catalyst is γ-AlOOH.

[0010] The second aspect of the present invention provides a material for processing and treating fossil energy, the material comprising a boehmite catalyst and fossil energy, the chemical formula of the boehmite catalyst being γ-AlOOH;

[0011] Wherein, the weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:1.

[0012] The third aspect of the present invention provides a method for processing and treating fossil energy, the method comprising: contacting a boehmite catalyst and a fossil energy in an atmosphere of oxygen-deficient, non-oxidizing gas or inert gas and performing a thermochemical conversion reaction to obtain a thermochemical conversion reaction product;

[0013] Wherein, the chemical formula of the boehmite catalyst is γ-AlOOH.

[0014] A fourth aspect of the present invention provides a method for processing and treating fossil energy in two stages, the method comprising: contacting a boehmite catalyst with a fossil energy in an atmosphere of anoxic, non-oxidizing gas or an inert gas, and subjecting the fossil energy to a thermochemical conversion reaction in a first stage and a second stage to obtain a thermochemical conversion reaction product;

[0015] Wherein, the temperature of the first stage is less than the temperature of the second stage; and the chemical formula of the boehmite catalyst is γ-AlOOH.

[0016] The fifth aspect of the present invention provides an application of a thermochemical conversion reaction product obtained by the method provided in the third aspect and the fourth aspect in the production of petroleum-like fuels and precious chemicals.

[0017] Through the above technical solution, the beneficial technical effects achieved by the present invention are as follows:

[0018] (1) In the technical solution provided by the present invention, on the one hand, the introduction of boehmite catalyst can significantly reduce the activation energy of the thermochemical conversion reaction of fossil energy (especially oil shale); on the other hand, the product can also be improved and modified through the thermochemical conversion reaction of fossil energy (especially oil shale), and the obtained catalytic thermochemical reaction product can be used to produce high-quality petroleum-like fuels or precious chemicals.

[0019] (2) The present invention uses a boehmite catalyst for the thermochemical conversion reaction of oil shale. After the introduction of the boehmite catalyst, the activation energy of the thermochemical conversion reaction of oil shale is reduced by 17.0%. In addition, the non-catalytic and catalytic systems of oil shale carry out two-stage thermochemical conversion reactions at lower and higher temperatures.

[0020] The inventors of the present invention have found that when oil shale is subjected to the first stage (e.g., 450°C) thermochemical conversion in the presence of a boehmite catalyst, the contents of O-, N-, S-containing compounds and long-chain aliphatic hydrocarbons are reduced by 69.9%, 42.4%, 20.4% and 41.5%, respectively, compared with the non-catalytic system of oil shale. In addition, the content of hydrocarbon compounds increased by 56.8%, which is conducive to the production of high-quality petroleum-like fuels; at the same time, the content of short-chain aliphatic hydrocarbons increased significantly by 158.7%, which is conducive to the lightening of oil products. The inventors of the present invention have noticed that the content of α-olefins, which are valuable units for the production of multifunctional polyolefins, increased by 27.9%. In addition, the contents of tridecane and tetradecane increased by 46.2% and 50.0%, respectively. Tridecane and tetradecane are one of the liquid alkanes widely used in academia and industry, and are often used as organic solvents and phase change materials, etc., and have important application value. What is even more surprising is that the content of branched alkanes increased by 180.6%. Branched alkanes usually have higher octane numbers. Compared with some π-system aromatic hydrocarbon compounds that can regulate octane numbers, branched alkanes are green octane regulators. In addition, branched alkanes are also surfactant precursors with good water solubility. Among them, monomethyl branched alkanes increased by 826.7%, which are functional anionic surfactant precursors with good water solubility and excellent cold water / hard water properties; dimethyl branched alkanes and trimethyl branched alkanes increased by 393.2%, which are green high-octane regulators, hydrocarbon fuels with good antifreeze properties or additives for advanced lubricants.

[0021] In addition, when oil shale is subjected to the second stage (e.g., 585°C) thermochemical conversion reaction in the presence of boehmite catalyst, the contents of O-, N-, S-containing compounds and long-chain aliphatic hydrocarbons are reduced by 64.7%, 25.0%, 8.2%, and 7.3%, respectively, compared with the non-catalytic system of oil shale, and the relative content of hydrocarbon compounds increases from 56.2% to 68.1%. At the same time, the content of short-chain aliphatic hydrocarbons increases by 34.7%, which is conducive to the formation of light petroleum fuels. Similar to the thermochemical conversion reaction in the first stage, after the introduction of boehmite, the content of branched alkanes increases by 50.0%, and the content of α-olefins increases by 24.8%. More importantly, the contents of benzene, toluene, xylene, and trimethylbenzene increase by 87.5%, 64.3%, 14.3%, and 25.0%, respectively. As important basic raw materials in the petrochemical industry, their market size is second only to ethylene and propylene. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 A is the PXRD diffraction pattern of the boehmite catalyst; Figure 1 B is the Py-FTIR image of the boehmite catalyst;

[0023] Figure 2 A is the TG curve of the original oil shale thermochemical conversion system without boehmite catalyst at different heating rates; Figure 2 B is the DTG curve of the original oil shale thermochemical conversion system without boehmite catalyst at different heating rates; Figure 2 C is the TG curve of the oil shale thermochemical conversion system containing boehmite catalyst at different heating rates; Figure 2 D is the DTG curve of the oil shale thermochemical conversion system containing boehmite catalyst at different heating rates;

[0024] Figure 3 A and Figure 3 B are the TG curves and DTG curves of different oil shale systems at a heating rate of 10K / min; Figure 3 C and Figure 3 D are the TG curves and DTG curves of different oil shale systems at a heating rate of 15K / min; Figure 3 E and Figure 3 F are the TG curves and DTG curves of different oil shale systems at a heating rate of 20 K / min; Figure 3 G and Figure 3 H are the TG curves and DTG curves of different oil shale systems at a heating rate of 25 K / min; Figure 3 I and Figure 3 J are the TG curves and DTG curves of different oil shale systems at a heating rate of 30 K / min;

[0025] Figure 4 A is the original oil shale system without boehmite catalyst based on the Starink approximate equation fitting and 1 / T α The regression plot of ; Figure 4 B is the oil shale system containing boehmite catalyst based on the Starink approximate equation fitting and 1 / T α The regression plot of ; Figure 4 C is based on the different oil shale thermochemical conversion systems obtained by Starink method, E α Distribution plot as a function of α;

[0026] Figure 5 A is the Py-EGA-MS diagram of different oil shale systems; Figure 5 B is the MS graph obtained from the products generated in the first peak region of different systems; Figure 5 C is the MS graph of the products generated in the second peak region by different systems;

[0027] Figure 6 A is the TIC diagram of the products produced by the first stage thermal conversion reaction of different oil shale systems; Figure 6 B is a schematic diagram of the distribution of hydrocarbons and non-hydrocarbon compounds in different oil shale systems after the first stage thermal conversion reaction;

[0028] Figure 7 A-7D is a schematic diagram of the distribution of various components in the products of the first stage thermal conversion reaction of different oil shale systems;

[0029] Figure 8 A is the TIC diagram of the products produced by the second stage thermal conversion reaction of different oil shale systems; Figure 8 B is a schematic diagram of the distribution of hydrocarbons and non-hydrocarbon compounds in different oil shale systems after the second stage thermal conversion reaction;

[0030] Fig. 9 A-9D is a schematic diagram of the distribution of various components in the products of the second-stage thermal conversion reaction of different oil shale systems. DETAILED DESCRIPTION

[0031] The endpoints and any values ​​of the ranges disclosed in this article are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0032] A first aspect of the present invention provides a boehmite catalyst for use in processing and treating fossil energy, wherein the chemical formula of the boehmite catalyst is γ-AlOOH.

[0033] The inventors of the present invention have found that in the thermochemical conversion reaction of fossil energy (especially oil shale), the L-acid and / or B-acid of the catalyst can serve as catalytic active sites. Combined with the Py-FTIR characterization results, it is shown that the intensity and concentration of the L-acid site of the boehmite catalyst are significantly higher than the intensity and concentration of the B-acid site, so that it has good catalytic performance for the thermochemical conversion of fossil energy (especially oil shale); the synergistic and competitive effects of these two acid sites can guide the thermochemical conversion reaction to occur preferentially along a specific path, giving boehmite excellent catalytic performance; in addition, the pore volume and surface area of ​​the boehmite catalyst are relatively large, and its internal pores are relatively abundant, which may also make boehmite have good catalytic performance.

[0034] In some embodiments of the present invention, preferably, in the boehmite catalyst, 0 μmol / g<B-acid concentration≤1×10 5 μmol / g, 0μmol / g<L-acid concentration≤1×10 5 μmol / g; further preferably, 0.1 μmol / g≤B-acid concentration≤100 μmol / g, 0.1 μmol / g≤L-acid concentration≤1000 μmol / g; more preferably, 0.1 μmol / g≤B-acid concentration≤10 μmol / g, 0.1 μmol / g≤L-acid concentration≤100 μmol / g; most preferably, 0.1 μmol / g≤B-acid concentration≤2 μmol / g, 10 μmol / g≤L-acid concentration≤100 μmol / g. In the present invention, B-acid is Acid; L-acid is Lewis acid.

[0035] In some embodiments of the present invention, preferably, in the boehmite catalyst, 0 cm 3 / g<Pore volume≤8000cm 3 / g,0m 2 / g<Specific surface area≤1×10 4 m 2 / g, 0nm<pore size≤1000nm; further preferably, 0.1cm 3 / g≤pore volume≤100cm 3 / g,0.1m 2 / g≤Specific surface area≤1000m 2 / g, 0.1nm≤pore size≤100nm; more preferably, 0.1cm 3 / g≤pore volume≤10cm 3 / g,0.1m2 / g≤Specific surface area≤500m 2 / g, 0.1nm≤pore size≤50nm; most preferably, preferably, 0.1cm 3 / g≤pore volume≤2cm 3 / g,0.1m 2 / g≤Specific surface area≤300m 2 / g, 0.1nm≤pore size≤20nm.

[0036] In some embodiments of the present invention, preferably, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale.

[0037] In the present invention, the selection range of the processing and treatment method is relatively wide. Preferably, the processing and treatment method is thermochemical conversion.

[0038] The boehmite catalyst studied in the present invention is used for processing and treating fossil energy, especially oil shale. Compared with the prior art, after introducing the boehmite catalyst into the thermochemical conversion system, the activation energy of the thermochemical conversion reaction can be significantly reduced. The product can also be improved and modified through the thermochemical conversion reaction of fossil energy (especially oil shale) to produce high-quality petroleum-like fuels or precious chemicals.

[0039] In the present invention, unless otherwise specified, the activation energy parameter of thermochemical conversion is obtained through the relationship curve between the weight loss rate and temperature of materials such as fossil energy.

[0040] In the present invention, unless otherwise specified, the activation energy change rate parameter is obtained by analyzing the relationship curves between the weight loss rate and temperature of a thermochemical conversion system containing a boehmite catalyst and a thermochemical conversion system not containing a boehmite catalyst, thereby obtaining the thermochemical conversion activation energy of each system, and by comparing and analyzing the activation energies of the thermochemical conversion system containing a boehmite catalyst and the thermochemical conversion system not containing a boehmite catalyst.

[0041] The second aspect of the present invention provides a material for processing and treating fossil energy, characterized in that the material comprises a boehmite catalyst and fossil energy, and the chemical formula of the boehmite catalyst is γ-AlOOH;

[0042] Wherein, the weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:1.

[0043] In the present invention, unless otherwise specified, the weight ratio of the boehmite catalyst to the fossil energy refers to the feed ratio of the boehmite catalyst to the fossil energy in terms of γ-AlOOH.

[0044] In some embodiments of the present invention, preferably, the weight ratio of the boehmite catalyst to the fossil energy is 1:1000 to 1:1.

[0045] In the present invention, in the boehmite catalyst, the B-acid concentration, L-acid concentration, pore volume, specific surface area and pore size are all in accordance with the above-mentioned definitions, and the present invention will not elaborate on them here.

[0046] In some embodiments of the present invention, preferably, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale.

[0047] The third aspect of the present invention provides a method for processing and treating fossil energy, the method comprising: contacting a boehmite catalyst and a fossil energy in an atmosphere of oxygen-deficient, non-oxidizing gas or inert gas and performing a thermochemical conversion reaction to obtain a thermochemical conversion reaction product;

[0048] Wherein, the chemical formula of the boehmite catalyst is γ-AlOOH.

[0049] In the present invention, the use of boehmite catalysts to perform thermochemical conversion on reactants can significantly reduce the activation energy of the thermochemical conversion reaction, and can also improve the quality of products through thermochemical conversion reactions of fossil energy (especially oil shale) to produce high-quality petroleum-like fuels or precious chemicals. In the present invention, the reactants include substances such as fossil energy.

[0050] In some embodiments of the present invention, preferably, the method comprises the following steps:

[0051] (1) mixing the boehmite catalyst and a fossil energy source in an atmosphere of oxygen-deficient, non-oxidizing gas or inert gas to obtain a mixture;

[0052] (2) The mixture is subjected to the thermochemical conversion reaction in an atmosphere lacking oxygen, a non-oxidizing gas or an inert gas.

[0053] In the present invention, the above-mentioned thermochemical conversion method can significantly reduce the activation energy of the thermochemical conversion reaction, and can also improve the quality of the product through the thermochemical conversion reaction of fossil energy (especially oil shale) to produce high-quality petroleum-like fuels or precious chemicals.

[0054] In the present invention, in step (1), the range of selection of the mixing method is relatively wide, and the boehmite catalyst and the fossil energy can be mixed evenly. In some embodiments of the present invention, the mixing method is selected from grinding and soaking.

[0055] In some embodiments of the present invention, the mixing time is generally 0 to 48 hours, for example 0h, 1h, 5h, 15h, 20h, 25h, 30h, 35h, 40h, 45h, 48h, and any value within the range of any two of the above values, preferably 0 to 5h.

[0056] In some embodiments of the present invention, the boehmite catalyst is mixed with fossil energy in the form of solid powder and ground to obtain a solid powder with an average particle size of 0.0001 to 1×10 11 μm; wherein the average particle size of the fossil energy or boehmite catalyst is 0.0001 to 5×10 5 μm, preferably 0.005 to 800 μm.

[0057] In the present invention, unless otherwise specified, when the thermochemical conversion reaction is carried out on the ground, there are certain requirements for the average particle size of the fossil energy or the boehmite catalyst, that is, the average particle size of the fossil energy and the boehmite catalyst is independently 0.0001 to 5×10 5 When the thermochemical conversion reaction is carried out underground, there is no special requirement for the average particle size of the boehmite catalyst. The main reason is that when the thermochemical conversion reaction is carried out underground, the underground rocks are cracked mainly by underground fracturing or explosion, and the particle size range of the rocks can be hundreds of meters or even larger, which is equivalent to the formation of rocks of various sizes due to underground explosions, and the boehmite catalyst is attached to the surface of the rock that produces the dominant oil or gas channel underground.

[0058] In some embodiments of the present invention, preferably, the weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:1, preferably 1:1000 to 1:1. In the present invention, controlling the weight ratio within the above specific range can make the thermochemical conversion reaction proceed more completely.

[0059] In the present invention, in the boehmite catalyst, the B-acid concentration, L-acid concentration, pore volume, specific surface area and pore size are all in accordance with the above-mentioned definitions, and the present invention will not elaborate on them here.

[0060] In some embodiments of the present invention, preferably, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale.

[0061] In the present invention, the selection range of the thermochemical conversion reaction conditions is relatively wide.

[0062] In some embodiments of the present invention, preferably, the temperature of the thermochemical conversion reaction is 30-900°C, for example, 30°C, 50°C, 150°C, 200°C, 250°C, 300°C, 350°C, 400°C, 450°C, 500°C, 550°C, 650°C, 750°C, 850°C, 900°C, and any value within the range of any two of the above values, preferably 150-550°C.

[0063] In some embodiments of the present invention, preferably, the time of the thermochemical conversion reaction is 0.00001s to 6 years, for example, 0.00001s, 0.0001s, 0.01s, 0.1s, 0.5s, 1s, 2s, 6s, 10s, 1min, 6min, 1h, 6h, 12h, 1 day, 100 days, 1 year, 2 years, 3 years, 4 years, 5 years, 6 years, and any value within the range of any two of the above values, preferably 0.0001s to 2 years.

[0064] In some embodiments of the present invention, preferably, the heating rate of the thermochemical conversion reaction is 0 to 8500°C / s, such as 0°C / s, 5°C / s, 15°C / s, 25°C / s, 55°C / s, 150°C / s, 550°C / s, 1000°C / s, 1500°C / s, 2500°C / s, 3500°C / s, 4000°C / s, 4500°C / s, 5500°C / s, 6500°C / s, 7500°C / s, 8500°C / s, and any value within the range of any two of the above values, preferably 0 to 4000°C / s. In the present invention, 10K / min=1 / 6°C / s.

[0065] In the present invention, the conditions of the above-mentioned thermochemical conversion reaction are controlled within a specific range, so that the thermochemical conversion reaction can proceed more completely.

[0066] In the present invention, unless otherwise specified, the heating rate parameter of the thermochemical conversion reaction depends on the heating method. When the Curie point heating method is used, the heating rate can be as high as 8500°C / s, while when other heating methods are used, the heating rate can be as low as 0.00001°C / s. In addition, when the thermochemical conversion reaction is carried out at a constant temperature, the heating rate is 0°C / s.

[0067] In the present invention, unless otherwise specified, the time of the thermochemical conversion reaction depends on specific conditions. If the thermochemical conversion reaction is carried out underground, the time of the thermochemical conversion reaction can be as long as 0.1 to 6 years, or can be several days or several months.

[0068] In some embodiments of the present invention, preferably, the non-oxidizing gas is selected from at least one of gaseous water, hydrogen, carbon monoxide and carbon dioxide.

[0069] In some embodiments of the present invention, preferably, the inert gas is selected from at least one of nitrogen, helium, krypton, argon, xenon and neon, preferably nitrogen.

[0070] In a specific embodiment of the present invention, the oxygen-deficient atmosphere or non-oxidizing gas may be an underground oxygen-deficient environment.

[0071] In some embodiments of the present invention, preferably, the thermochemical conversion reaction is carried out above ground or underground.

[0072] In a specific embodiment of the present invention, when the thermochemical conversion reaction is carried out underground, the boehmite catalyst is directly transported to the underground reaction site, or the boehmite catalyst is transported to the underground reaction site via a fluid load. In the present invention, the fluid can be selected from a wide range of gases or liquids, such as air, nitrogen, carbon dioxide, helium, carbon monoxide, hydrogen, water, and organic solvents.

[0073] The method provided by the present invention uses the active component containing boehmite as a catalyst to undergo a thermochemical conversion reaction with the fossil energy (especially oil shale) in an atmosphere of anoxic, non-oxidizing gas or inert gas, which can significantly reduce the activation energy of the thermochemical conversion of the fossil energy (especially oil shale), and can also improve the quality of the product through the thermochemical conversion of the fossil energy (especially oil shale) to produce high-quality petroleum-like fuels or precious chemicals.

[0074] A fourth aspect of the present invention is a method for processing and treating fossil energy in two stages, the method comprising: contacting a boehmite catalyst with fossil energy in an atmosphere of anoxic, non-oxidizing gas or inert gas, and performing a thermochemical conversion reaction on the fossil energy in a first stage and a second stage to obtain a thermochemical conversion reaction product;

[0075] Wherein, the temperature of the first stage is less than the temperature of the second stage; and the chemical formula of the boehmite catalyst is γ-AlOOH.

[0076] In some embodiments of the present invention, preferably, the method comprises the following steps:

[0077] (1) mixing the boehmite catalyst and a fossil energy source in an atmosphere of oxygen-deficient, non-oxidizing gas or inert gas to obtain a mixture;

[0078] (2) Under an atmosphere lacking oxygen, a non-oxidizing gas or an inert gas, the mixture is subjected to a first-stage and a second-stage thermochemical conversion reaction.

[0079] Depending on the temperature of the thermochemical conversion reaction, high-quality petroleum-like fuels can be produced through thermochemical conversion reactions, the content of hydrocarbon compounds and short / medium-chain aliphatic hydrocarbons can be increased, the content of long-chain aliphatic hydrocarbons and heteroatom compounds can be reduced, or several valuable chemicals that have attracted widespread attention from academia and industry can be preferentially produced, such as branched-chain alkanes (monomethyl branched-chain alkanes, dimethyl branched-chain alkanes and trimethyl branched-chain alkanes), tridecane, tetradecane, α-olefins (especially 1-hexene), benzene, toluene, xylene and trimethylbenzene, etc.

[0080] In the present invention, in step (1), the range of selection of the mixing method is relatively wide, and the boehmite catalyst and the fossil energy can be mixed evenly. In some embodiments of the present invention, the mixing method is selected from grinding / immersion.

[0081] In some embodiments of the present invention, the mixing time is generally 0 to 48 hours, for example 0h, 1h, 5h, 15h, 20h, 25h, 30h, 35h, 40h, 45h, 48h, and any value within the range of any two of the above values, preferably 0 to 5h.

[0082] In some embodiments of the present invention, the boehmite catalyst is mixed with fossil energy in the form of solid powder and ground to obtain a solid powder with an average particle size of 0.0001 to 1×10 11 The average particle size of the fossil energy or boehmite catalyst is 0.0001 to 5×10 5 μm, preferably 0.005 to 800 μm.

[0083] In the present invention, unless otherwise specified, when the thermochemical conversion reaction is carried out on the ground, there are certain requirements for the average particle size of the fossil energy or the boehmite catalyst, that is, the average particle size of the fossil energy and the boehmite catalyst is independently 0.0001 to 5×10 5 When the thermochemical conversion reaction is carried out underground, there is no special requirement for the average particle size of the boehmite catalyst. The main reason is that when the thermochemical conversion reaction is carried out underground, the underground rocks are cracked mainly by underground fracturing or explosion, and the particle size range of the rocks can be hundreds of meters or even larger, which is equivalent to the formation of rocks of various sizes due to underground explosions, and the boehmite catalyst is attached to the surface of the rock that produces the dominant oil or gas channel underground.

[0084] In some embodiments of the present invention, preferably, the weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:1, preferably 1:1000 to 1:1. In the present invention, controlling the weight ratio within the above specific range can make the thermochemical conversion reaction proceed more completely.

[0085] In the present invention, in the boehmite catalyst, the B-acid concentration, L-acid concentration, pore volume, specific surface area and pore size are all in accordance with the above-mentioned definitions, and the present invention will not elaborate on them here.

[0086] In some embodiments of the present invention, preferably, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale.

[0087] In some embodiments of the present invention, preferably, the temperature of the first stage is 50-550°C, for example, 50°C, 150°C, 200°C, 250°C, 300°C, 350°C, 400°C, 450°C, 490°C, 550°C, and any value within the range of any two of the above values, preferably 150-490°C.

[0088] In some embodiments of the present invention, preferably, the temperature of the second stage is 200-620°C, for example, 200°C, 260°C, 300°C, 350°C, 400°C, 450°C, 500°C, 550°C, 600°C, 620°C, and any value within the range of any two of the above values, preferably 260-550°C.

[0089] In some embodiments of the present invention, preferably, the time of the first stage and the second stage are each independently 0.00001s to 6 years, for example, 0.00001s, 0.0001s, 0.01s, 0.1s, 0.5s, 1s, 2s, 6s, 10s, 1min, 6min, 1h, 6h, 12h, 1 day, 100 days, 1 year, 2 years, 3 years, 4 years, 5 years, 6 years, and any value within the range of any two of the above values, preferably 0.0001s to 2 years.

[0090] In some embodiments of the present invention, preferably, the heating rates of the first stage and the second stage are each independently 0 to 8500°C / s, for example, 0°C / s, 5°C / s, 15°C / s, 25°C / s, 55°C / s, 150°C / s, 550°C / s, 1000°C / s, 1500°C / s, 2500°C / s, 3500°C / s, 4000°C / s, 4500°C / s, 5500°C / s, 6500°C / s, 7500°C / s, 8500°C / s, and any value within the range of any two of the above values, preferably 0 to 4000°C / s.

[0091] In the present invention, the conditions of the first stage and the second stage are controlled within a specific range, so that the thermochemical conversion reaction can proceed more completely.

[0092] In the present invention, unless otherwise specified, the heating rate parameters of the first stage and the second stage depend on the heating method. When the Curie point heating method is used, the heating rate can be as high as 8500°C / s, while when other heating methods are used, the heating rate can be as low as 0.00001°C / s. In addition, when a constant temperature method is used for the thermochemical conversion reaction, the heating rate is 0°C / s.

[0093] In the present invention, unless otherwise specified, the duration of the first stage and the second stage depends on specific conditions. If the thermochemical conversion reaction is carried out underground, the duration of the first stage and the second stage can be 0.1 to 6 years, or can be a few days or a few months.

[0094] In some embodiments of the present invention, preferably, the non-oxidizing gas is selected from at least one of gaseous water, hydrogen, carbon monoxide and carbon dioxide.

[0095] In some embodiments of the present invention, preferably, the inert gas is selected from at least one of nitrogen, helium, krypton, argon, xenon and neon, preferably helium.

[0096] In a specific embodiment of the present invention, the oxygen-deficient atmosphere or non-oxidizing gas may be an underground oxygen-deficient environment.

[0097] In some embodiments of the present invention, preferably, the first stage and the second stage thermochemical conversion reactions are carried out above ground or underground.

[0098] In a specific embodiment of the present invention, preferably, when the thermochemical conversion reactions of the first stage and the second stage are carried out underground, the boehmite catalyst is directly transported to the underground reaction site, or the boehmite catalyst is transported to the underground reaction site through a fluid load. In the present invention, the selection range of the fluid is relatively wide, and it can be a liquid or a gas, for example, air, nitrogen, carbon dioxide, helium, carbon monoxide, hydrogen, water, and an organic solvent.

[0099] The method provided by the present invention uses an active component containing boehmite as a catalyst, and the boehmite catalyst is contacted with the fossil energy (especially oil shale) in an atmosphere of anoxic, non-oxidizing gas or inert gas, and the fossil energy is subjected to a thermochemical conversion reaction through a first stage and a second stage. According to different thermochemical conversion temperatures, high-quality petroleum-like fuels can be produced through thermochemical conversion, the content of hydrocarbon compounds and short / medium-chain aliphatic hydrocarbons can be increased, the content of long-chain aliphatic hydrocarbons and heteroatom compounds can be reduced, or several precious chemicals that have attracted widespread attention from academia and industry can be preferentially produced, such as branched alkanes (monomethyl branched alkanes, dimethyl branched alkanes and trimethyl branched alkanes), tridecane, tetradecane, α-olefins (especially 1-hexene), benzene, toluene, xylene and trimethylbenzene, etc.

[0100] The present invention will be described in detail below through examples.

[0101] Example 1

[0102] The boehmite catalyst with the chemical formula of γ-AlOOH was subjected to a powder X-ray diffraction (PXRD) test. The XRD diffraction pattern of the boehmite catalyst is as follows: Figure 1 As shown in A, Figure 1 A It can be seen that the diffraction peak of the above boehmite catalyst matches well with the diffraction peak of boehmite (JCPDS No. 21-1307), indicating that the catalyst is boehmite.

[0103] The boehmite catalyst was characterized by Fourier transform infrared spectroscopy (Py-FTIR) of pyridine adsorption to verify the presence of acid sites on its surface, such as Figure 1 As shown in B, when the desorption temperature is 200℃, at 1539cm -1 and 1450cm -1 The peaks at 1493 cm-1 are the absorption peaks of the B-acid and L-acid sites of pyridine adsorption. -1 The absorption peak at is the result of the interaction of pyridine molecules with B-acid and L-acid sites at the same time. This indicates that B-acid and L-acid sites exist in the above-mentioned boehmite catalyst. Calculations show that the concentrations of B-acid and L-acid sites are 0.64 μmol / g and 71.55 μmol / g, respectively. In addition, at a desorption temperature of 350°C, the concentration of B-acid sites slightly decreases to 0.6 μmol / g (a decrease of 6.25%), and the concentration of L-acid sites significantly decreases to 39.29 μmol / g (a significant decrease of 45.09%), indicating that the concentration / intensity of L-acid in boehmite catalyst is significantly higher / stronger than that of B-acid. Therefore, the synergistic and competitive effects of L-acid and B-acid in boehmite catalysts may guide the thermochemical conversion reaction of oil shale to occur preferentially along a specific path, giving boehmite catalysts excellent catalytic performance.

[0104] Meanwhile, the pore volume, surface area and pore diameter of the above boehmite are about 0.87 cm 3 / g, 295.92m 2 / g and 11.08nm. Therefore, the pore volume and surface area of ​​the boehmite catalyst are relatively large, and its internal pores are relatively abundant, which may also make boehmite produce good catalytic performance.

[0105] In order to evaluate the catalytic performance of boehmite catalyst for the thermochemical conversion reaction of oil shale, thermogravimetric (TG) analysis experiments were carried out with or without boehmite catalyst:

[0106] When a boehmite catalyst is involved, 10 mg of oil shale powder and 1 mg of boehmite powder samples with a particle size of less than 74 μm are spread in a crucible, and the heating rates are 10K / min (10K / min=1 / 6℃ / s, the same applies below), 15K / min, 20K / min, 25K / min and 30K / min, respectively, and the temperature is raised from 35℃ to 900℃. In addition, a high-purity dry nitrogen gas with a constant flow rate of 50 mL / min is used to provide an inert environment during the experiment, wherein the flow rates of the purge gas and the protective gas are both 25 mL / min. When there is no boehmite catalyst involved, except for the experiment of 10 mg of oil shale powder samples with a particle size of less than 74 μm, all other conditions are the same as the TG analysis experiment with the participation of the boehmite catalyst. Three TG experiments were performed on each sample to ensure the reliability and repeatability of the results.

[0107] The series of TG ( Figure 2 A. Figure 2 C) and DTG( Figure 2 B. Figure 2 D) The data was analyzed and processed. Figure 2 A and Figure 2 B are the TG and DTG curves obtained from the thermochemical conversion system of oil shale at a heating rate of 10-30K / min and without the participation of boehmite catalyst; Figure 2 C and Figure 2 D are the TG and DTG curves obtained from the thermochemical conversion system of oil shale when the heating rate is 10-30K / min and boehmite catalyst is involved; specifically:

[0108] When the heating rate is 10K / min, the TG curve of the original oil shale system obtained by thermochemical conversion ( Figure 3 A) is mainly divided into three stages; the first stage is mainly before 200℃, the weight loss rate in this stage is 0.2%, and there is no obvious peak in the corresponding DTG curve ( Figure 3B), this stage is mainly due to the volatilization of trace interlayer water or a small amount of water in inorganic minerals; the temperature range of the second stage is mainly 200-600℃, and its weight loss rate is 15.4%. There is an obvious peak in the DTG curve corresponding to this stage ( Figure 3 B), which is mainly due to the thermochemical conversion of organic matter in oil shale; the third stage is mainly after 600℃, the weight loss rate in this stage is 25.7%, and there is also an obvious peak in the corresponding DTG curve ( Figure 3 B), which is mainly related to the thermochemical transformation of inorganic minerals in oil shale.

[0109] like Figure 3 As shown in Figures 3A and 3B, the TG and DTG curves obtained by thermochemical conversion of the oil shale system with the introduction of boehmite catalyst are almost similar to those obtained by the thermochemical conversion system of the original oil shale, but there are also the following three main differences: (1) The mass loss in the second stage is mainly attributed to the thermochemical conversion of organic matter in the oil shale. In the TG curve at the same temperature, after the introduction of the boehmite catalyst, the mass loss in the thermochemical conversion system of the oil shale becomes larger; (2) After the introduction of the boehmite catalyst, the temperature corresponding to the maximum mass loss rate in the thermochemical conversion system of the oil shale (T max ) from 432.4℃ to 427.9℃; (3) After the introduction of boehmite catalyst, the total mass loss in the thermochemical conversion system of oil shale is greater.

[0110] At the same time, when the heating rate is 15( Figure 3 C and Figure 3 D) 20( Figure 3 E and Figure 3 F), 25( Figure 3 G and Figure 3 H) and 30( Figure 3 I and Figure 3 When the boehmite catalyst was introduced into the system, the change trends of TG and DTG curves of the thermochemical conversion of oil shale were almost similar, which indicated that the boehmite catalyst could be used as a catalyst to promote the thermochemical conversion of oil shale.

[0111] Based on TG analysis, the catalytic performance of boehmite catalyst for oil shale thermochemical conversion reactions was evaluated using the Starink method, such as Figure 4 A. Figure 4 B and Figure 4 C, where the oil shale thermochemical conversion system without and with boehmite catalyst is as follows: Figure 4 A. Figure 4 B, after the introduction of boehmite catalyst, such as Figure 4As shown in C, the Starink method evaluation shows that the activation energy of the thermochemical conversion reaction of oil shale is reduced by 17.0%, wherein the approximate equations of the Starink method are shown in formula (1):

[0112]

[0113] At the same time, we conducted temperature programmable pyrolyzer (Py-EGA-MS) experiments without or with boehmite catalyst: when boehmite was present, 1 mg of oil shale with an average particle size of less than 74 μm and 0.1 mg of boehmite catalyst powder were spread in the sample cup, the heating rate was 10 K / min, the temperature was raised from 55 ° C to 850 ° C, the carrier gas was dry high-purity helium, the total flow rate was 12.1 mL / min, of which the column flow rate and purge flow rate were 0.82 mL / min and 3 mL / min, respectively. In addition, the column head pressure was 80 kPa, the column box, gas chromatography column (without stationary phase), gas chromatography (GC) and mass spectrometry (MS) injection port temperature were all 300 ° C, and the m / z range was 10-800. When there was no boehmite catalyst, except for the experiment of 1 mg of oil shale powder with a particle size of less than 74 μm, other conditions were the same as the Py-EGA-MS analysis experiment with this catalyst. Py-EGA-MS experiments were performed three times for each sample to ensure the reliability and reproducibility of the results.

[0114] Due to the lack of separation columns, the products obtained could not be separated and identified by Py-EGA-MS experiments. However, some qualitative information about the product composition can be obtained from the MS graphs that extract the desired thermochemical conversion region. We studied the Py-EGA-MS curves ( Figure 5 A) shows that after the oil shale is thermochemically converted, two peaks are obtained. The front peak corresponds to the decomposition of organic matter, and the back peak corresponds to the decomposition of inorganic matter. After the introduction of the boehmite catalyst, the highest point of the organic matter peak obviously moves to the low temperature zone, and the peak intensity of the total ion chromatogram increases, which shows that after the introduction of the boehmite catalyst, it can indeed play a catalytic role and convert more organic matter into oil and gas products. For example, the Py-EGA-MS curve ( Figure 5 As shown in A), the signal in the MS graph obtained from the product generated from the first peak region is complex but obvious, such as Figure 5B. The analysis shows that we can clearly distinguish the mass fragments of m / z = 41 + 14n (n = 0, 1, 2, 3, etc.) and 43 + 14n (n = 0, 1, 2, 3, etc.), which are usually characteristic ion fragments of aliphatic hydrocarbons. At the same time, we can also observe ion fragments of m / z 109 and 95, which are usually fragments of aromatic compounds, and ion fragments of m / z = 81, which can be attributed to fragments of alkyl-substituted cyclohexene. The MS graph obtained by extracting the product in the second peak area ( Figure 5 C), signals with m / z values ​​of 44, 28, 16, and 12 can be obtained, which are typical MS signals of CO2, while the signals of other fragments are extremely weak. These facts confirm that the DTG curve ( Figure 3 The first and second peaks of B) are mainly due to the thermochemical transformation of organic and inorganic substances in oil shale, respectively.

[0115] To further explore the catalytic effect of the above-mentioned boehmite on the thermochemical conversion of oil shale, we also analyzed the distribution of the products of the rapid thermochemical conversion reaction by rapid pyrolysis gas chromatography-mass spectrometry (Py-GC-MS). During the Py-GC-MS experiment, dry high-purity helium was used to purge the volatiles produced in the pyrolyzer, with a total flow rate of 18.1 mL / min, and a small portion of helium flow rate introduced into the fused silica GC column after separation was 1.37 mL / min, with an m / z range of 50-550, and a mass ratio of oil shale to boehmite of 10:1. In order to achieve rapid thermochemical conversion, the oil shale sample with or without boehmite catalyst was placed in a sample cup, and then placed in a pyrolysis furnace at a preset temperature, and the sample was pyrolyzed for 6 seconds at this preset temperature. During the experiment, the temperature of the GC column was first set to 50 °C and maintained at this temperature for 5 min. Then, the thermochemical conversion temperature was increased from 50 °C to 250 °C at a heating rate of 3 °C / min and maintained at 250 °C for 20 min. Three Py-GC-MS experiments were performed for each sample to ensure the reliability and repeatability of the results. The chromatographic peaks observed in the total ion chromatogram (TIC) were qualitatively matched by comparing the peaks in the MS spectrum with those in the National Institute of Standards and Technology (NIST) mass spectral database. The chromatographic peak area integration and data analysis were performed using GC-MS Postrun Analysis (GCMSsolution Version 4.3) software.

[0116] The non-catalytic and catalytic systems of oil shale were subjected to two-stage thermochemical conversion reactions at lower and higher temperatures, respectively. When oil shale was subjected to the first stage (e.g., 450°C) thermochemical conversion in the presence of a boehmite catalyst, the intensity and number of chromatographic peaks increased compared to the non-catalytic system of oil shale ( Figure 6A). In addition, the content of hydrocarbon compounds increased by 56.8% ( Figure 6 B), the content of non-hydrocarbon compounds was significantly reduced by 60.1% ( Figure 6 B). Further analysis showed that the contents of O-, N-, and S-containing compounds decreased by 69.9%, 42.4%, and 20.4%, respectively ( Figure 7 A), the contents of paraffins, alkenes and aromatics increased by 81.0%, 85.7% and 4.4% respectively ( Figure 7 A), which is conducive to the production of high-quality petroleum-like fuels. The contents of tridecane and tetradecane increased by 46.2% and 50.0% respectively ( Figure 7 B). Tridecane and tetradecane are among the liquid alkanes widely used in academia and industry. They are often used as organic solvents and phase change materials, and have important application value. In addition, we noticed that the content of α-olefins, which are valuable units for producing various functional polyolefins, increased by 27.9% ( Figure 7 B), to our surprise, the content of linear alkanes decreased by 9.0% ( Figure 7 B), while the content of branched alkanes increased by 180.6% ( Figure 7 B). Branched alkanes usually have a higher octane number. Compared with some π-system aromatic compounds that can regulate the octane number, they are a green octane number regulator. In addition, branched alkanes are also a surfactant precursor with good water solubility. Monomethyl branched alkanes increased by 826.7% ( Figure 7 C), which is a functional anionic surfactant precursor with good water solubility and excellent cold water / hard water performance. Dimethyl branched alkanes and trimethyl branched alkanes increased by 393.2% ( Figure 7 C), they are green high-octane regulators, hydrocarbon fuels with good antifreeze properties, or additives for advanced lubricants. Further analysis shows that short-chain (≤C 13 ) and medium chain (C 14 -C 19 ) the content of aliphatic hydrocarbons increased by 158.7% and 83.0% respectively ( Figure 7 D), long chain (C 20 -C 25 and ≥C 26 ) The content of aliphatic hydrocarbons decreased by 41.5% ( Figure 7 D), which is conducive to making the oil lighter.

[0117] In addition, when oil shale is subjected to the second stage (e.g., 585°C) thermochemical conversion reaction in the presence of boehmite, the intensity and number of chromatographic peaks also increase compared to the non-catalytic system of oil shale ( Figure 8 A). In addition, the content of hydrocarbon compounds increased to 21.2% ( Figure 8B), the content of non-hydrocarbon compounds was significantly reduced by 27.2% ( Figure 8 B). Further analysis showed that the contents of O-, N- and S-containing compounds decreased by 64.7%, 25.0% and 8.2%, respectively ( Fig. 9 A), the contents of paraffins, olefins and aromatics increased by 1.7%, 34.2% and 24.4% respectively ( Fig. 9 A), therefore, this boehmite catalyst has a good quality improvement effect at high temperature. Similar to the thermochemical conversion reaction in the first stage, after the introduction of boehmite, the content of straight-chain alkanes decreased by 4.8% ( Fig. 9 B), the content of branched alkanes increased by 50.0% ( Fig. 9 B), the α-olefin content increased by 24.8% ( Fig. 9 B), where the content of 1-hexene, a typical α-olefin, increased by 25.0% ( Fig. 9 B). In addition, the content of monocyclic aromatic hydrocarbons increased by 30.2% ( Fig. 9 C), while the content of PAHs decreased by 15.4% ( Fig. 9 C). This is because coke is mainly formed by further aromatization of polycyclic aromatic hydrocarbons during the thermochemical conversion of oil shale, which is a very large carbonaceous material that is difficult to decompose. This proves that boehmite has certain anti-coking properties. More importantly, the contents of benzene, toluene, xylene and trimethylbenzene increased by 87.5%, 64.3%, 14.3% and 25.0% respectively ( Fig. 9 C), they are important basic raw materials in the petrochemical industry, and their market size is second only to ethylene and propylene. 13 ) and medium chain (C 14 ~C 19 ) The content of aliphatic hydrocarbons increased by 34.7% and 7.3% respectively ( Fig. 9 D), long chain (C 20 -C 25 and ≥C 26 ) The content of aliphatic hydrocarbons decreased by 7.3% ( Fig. 9 D), which is conducive to the formation of light petroleum fuels.

[0118] Therefore, when we use relatively cheap boehmite as a catalyst, the activation energy of thermochemical conversion of oil shale can be reduced by 17.0%, which can reduce costs and energy consumption. The research results show that it is possible to achieve quality modification and anti-coking, and depending on the different thermochemical conversion temperatures, it is possible to produce high value-added platform chemicals, such as branched alkanes (e.g., monomethyl, dimethyl and trimethyl branched alkanes), tridecane, tetradecane, α-olefins (especially 1-hexene), benzene, toluene, xylene and trimethylbenzene. The pore volume and surface area of ​​boehmite catalysts are relatively large, and their internal pores are relatively rich, which may give boehmite good catalytic performance. In addition, the intensity and concentration of L-acid sites are significantly higher than those of B-acid sites, and their competition and synergistic effects may be the scientific basis for their catalytic performance.

[0119] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A boehmite catalyst for use in processing and treating fossil energy, wherein: The chemical formula of the boehmite catalyst is γ-AlOOH.

2. The use according to claim 1, wherein: In the boehmite catalyst, 0 μmol / g<B-acid concentration≤1×10 5 μmol / g, 0μmol / g<L-acid concentration≤1×10 5 μmol / g; And / or, in the boehmite catalyst, 0cm 3 / g<Pore volume≤8000cm 3 / g,0m 2 / g<Specific surface area≤1×10 4 m 2 / g, 0nm<pore size≤1000nm; And / or, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale.

3. A material for processing and treating fossil energy, characterized in that: The materials include a boehmite catalyst and fossil energy, and the chemical formula of the boehmite catalyst is γ-AlOOH; Wherein, the weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:

1.

4. The material according to claim 3, wherein in, The weight ratio of the boehmite catalyst to the fossil energy is 1:1000 to 1:1; and / or, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale; and / or, in the boehmite catalyst, 0 μmol / g<B-acid concentration≤1×10 5 μmol / g, 0μmol / g<L-acid concentration≤1×10 5 μmol / g; And / or, in the boehmite catalyst, 0cm 3 / g<Pore volume≤8000cm 3 / g,0m 2 / g<Specific surface area≤1×10 4 m 2 / g, 0nm<pore size ≤1000nm.

5. A method for processing and treating fossil energy, characterized in that: The method comprises: contacting a boehmite catalyst with a fossil energy source in an atmosphere of oxygen-deficient, non-oxidizing gas or inert gas and performing a thermochemical conversion reaction to obtain a thermochemical conversion reaction product; Wherein, the chemical formula of the boehmite catalyst is γ-AlOOH.

6. The method according to claim 5, wherein: The weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:1, preferably 1:1000 to 1:1; and / or, in the boehmite catalyst, 0 μmol / g<B-acid concentration≤1×10 5 μmol / g, 0μmol / g<L-acid concentration≤1×10 5 μmol / g; And / or, in the boehmite catalyst, 0cm 3 / g<Pore volume≤8000cm 3 / g,0m 2 / g<Specific surface area≤1×10 4 m 2 / g, 0nm<pore size≤1000nm; And / or, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale.

7. The method according to claim 5 or 6, wherein: The conditions of the thermochemical conversion reaction include: temperature of 30 to 900°C, preferably 150 to 550°C; time of 0.00001s to 6 years, preferably 0.0001s to 2 years; heating rate of 0 to 8500°C / s, preferably 0 to 4000°C / s; and / or, the non-oxidizing gas is selected from at least one of gaseous water, hydrogen, carbon monoxide and carbon dioxide; And / or, the thermochemical conversion reaction is carried out above ground or underground; and / or, when the thermal conversion reaction is carried out on the ground, the average particle size of the fossil energy and the boehmite catalyst is independently 0.0001 to 5×10 5 μm, preferably 0.005 to 800 μm.

8. A method for processing and treating fossil energy in two stages, characterized in that: The method comprises: contacting a boehmite catalyst with a fossil energy source in an atmosphere of oxygen-deficient, non-oxidizing gas or inert gas, and performing a thermochemical conversion reaction on the fossil energy source through a first stage and a second stage to obtain a thermochemical conversion reaction product; Wherein, the temperature of the first stage is less than the temperature of the second stage; and the chemical formula of the boehmite catalyst is γ-AlOOH.

9. The method according to claim 8, wherein: The weight ratio of the boehmite catalyst to the fossil energy is 1:6000 to 15:1, preferably 1:1000 to 1:1; and / or, in the boehmite catalyst, 0 μmol / g<B-acid concentration≤1×10 5 μmol / g, 0μmol / g<L-acid concentration≤1×10 5 μmol / g; And / or, in the boehmite catalyst, 0cm 3 / g<Pore volume≤8000cm 3 / g,0m 2 / g<Specific surface area≤1×10 4 m 2 / g, 0nm<pore size≤1000nm; and / or, the fossil energy is selected from at least one of shale oil, oil shale, heavy oil, oil sands, coal and petroleum, preferably oil shale; And / or, the conditions of the thermochemical conversion reaction include: the temperature of the first stage is 50-550°C, preferably 150-490°C; the temperature of the second stage is 200-620°C, preferably 260-550°C; the time of the first stage and the second stage is independently 0.00001s-6 years, preferably 0.0001s-2 years; the heating rate of the first stage and the second stage is independently 0-8500°C / s, preferably 0-4000°C / s; And / or, the non-oxidizing gas is selected from at least one of gaseous water, hydrogen, carbon monoxide and carbon dioxide.

10. Use of the thermochemical conversion reaction product obtained by the method according to any one of claims 5 to 9 in the production of petroleum-like fuels and precious chemicals.

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