Blended gasoline as well as preparation method and application thereof

Abstract

The invention provides blended gasoline as well as a preparation method and application thereof. The blended gasoline comprises the following components in percentage by weight: 40-60% of mixed light hydrocarbon, 25-40% of direct coal liquefaction naphtha and 8-22% of methyl tert-butyl ether, wherein the mixed light hydrocarbon is fraction hydrocarbon prepared by rectifying MTP byproduct mixed aromatic hydrocarbon, and the distillation range of the mixed light hydrocarbon is less than or equal to 165 DEG C. The finished product blended gasoline fully combines the advantages of the mixed light hydrocarbon with the distillation range of less than or equal to 165 DEG C, the direct coal liquefaction naphtha and the methyl tert-butyl ether in the MTP byproduct mixed aromatic hydrocarbon, realizes value-added utilization of the MTP byproduct mixed aromatic hydrocarbon, has the advantages of low colloid and mechanical impurity content and low sulfur content, can fully burn and release high heat value when being applied to the field of automobiles, and has the advantages of low energy consumption and low cost. Sediments generated during combustion are few, the content of sulfide in tail gas is low, and pollution to the environment is small.

Description

Technical Field

[0001] The present invention relates to the technical field of coal chemical industry, and in particular to a blended gasoline, a preparation method and application thereof. Background Art

[0002] The existing technology uses the methanol to propylene process (MTP) of Lurgi Company in Germany to produce mixed aromatics as by-products. The main components of the mixed aromatics are alkanes, cycloalkanes, olefins and aromatics. According to the different catalyst cycles, the aromatic content is generally 20-60%. The impurity content in the mixed aromatics is low, the benzene content is negligible (<0.5%), the S and N content is low (<1ppm), and the octane number is above 96. However, the induction period and actual colloid (an indicator of the oxidation stability of automotive gasoline) of the mixed aromatics do not meet the requirements of the National VI standard, and the added value is lower than that of finished diesel, and it is necessary to improve its quality and efficiency.

[0003] Invention patent CN 114181735 A discloses a blended gasoline and a production method thereof, the method comprising: (1) treating a mixed aromatic hydrocarbon by-product of a methanol to propylene process and / or a C 9+ The oil product is subjected to selective diolefin hydrogenation reaction to obtain a mixed hydrocarbon stream: the mixed hydrocarbon stream is subjected to a first distillation to obtain C 12 The following components: (2) C 12 The following components are mixed with the C6 and above components in the mixed benzene produced by the naphtha steam cracking process and the alkylate oil produced by the alkylation reaction of liquefied petroleum gas to obtain blended gasoline.

[0004] Invention patent CN 112322343 A discloses a method and device for reforming MTP byproduct sludge mixed aromatics to produce high aromatic content gasoline, a high aromatic content gasoline and its application. The method comprises the following steps: (1) distilling the MTP byproduct mixed aromatics to obtain heavy components and mixed light hydrocarbons with a distillation range of <165°C; (2) in the presence of an aromatization catalyst, heating the mixed light hydrocarbons to carry out an aromatization reaction, and cooling the obtained aromatized product to obtain a gas phase component and high aromatic content gasoline.

[0005] Existing mixed aromatics upgrading technologies, such as selective hydrogenation + octane recovery technology (ULSO technology), selective hydrogenation + aromatization technology, Fischer-Tropsch synthesis to olefins (GTO) technology, etc., all have the disadvantages of complex process flow and high cost, and cannot achieve the value-added utilization of mixed aromatics. Summary of the invention

[0006] The main purpose of the present invention is to provide a blended gasoline, a preparation method and application thereof, so as to solve the problems of poor performance and low added value of MTP by-product mixed aromatics in the prior art.

[0007] In order to achieve the above object, according to one aspect of the present invention, a blended gasoline is provided. The blended gasoline comprises, by weight percentage, 40-60% of mixed light hydrocarbons, 25-40% of coal direct liquefaction naphtha and 8-22% of methyl tert-butyl ether; wherein the mixed light hydrocarbons are fraction hydrocarbons obtained by distillation of MTP by-product mixed aromatic hydrocarbons, and the distillation range of the mixed light hydrocarbons is ≤165°C.

[0008] Furthermore, the mixed light hydrocarbons include, by weight, 30 to 51 parts of olefins, 10 to 30 parts of aromatics, 8 to 25 parts of cycloalkanes, 4 to 10 parts of normal alkanes, 18 to 38 parts of isoalkanes, 0 to 0.01 parts of mechanical impurities and colloids, and the mass concentration of the colloids is less than 80 mg / 100 mL; wherein the olefins include monoolefins and diolefins, and the weight ratio of the two is (96.7 to 100):(0 to 3.3).

[0009] Furthermore, the blended gasoline includes, by weight percentage, 45-55% of mixed light hydrocarbons, 30-40% of coal direct liquefaction naphtha and 10-20% of methyl tert-butyl ether.

[0010] According to another aspect of the present invention, a method for preparing the above-mentioned blended gasoline is provided, comprising the following steps: step S1, distilling the MTP by-product mixed aromatic hydrocarbons to obtain mixed light hydrocarbons, wherein the distillation range of the mixed light hydrocarbons is ≤165°C; step S2, mixing coal direct liquefaction naphtha, methyl tert-butyl ether and the mixed light hydrocarbons to obtain blended gasoline.

[0011] Further, in step S1, the MTP by-product mixed aromatic hydrocarbons include 20 to 46.5 parts of olefins, 20 to 60 parts of aromatics, 6 to 15 parts of cycloalkanes, 2 to 5 parts of normal alkanes, 18 to 35 parts of isoalkanes, 0.01 to 0.5 parts of mechanical impurities and the remainder of colloid, and the mass concentration of the colloid is 110 to 220 mg / 100 mL; wherein the olefins include monoolefins and diolefins, and the weight ratio of the two is (92.5 to 99.957): (0.043 to 7.5); and / or the distillation is carried out in a distillation tower, the number of theoretical plates of the distillation tower is 15 to 30, the reflux ratio is (1 to 10): 1, the extraction rate is 10 to 20 mL / min, the heating rate is 0.5 to 8°C / min, and the top pressure is 0.1 to 0.5 MPa.

[0012] Furthermore, in step S2, the mixing method includes one or more of mechanical stirring, compressed air stirring, pump circulation and pipeline blending.

[0013] Furthermore, step S2 also includes the following steps: step S21, in a hydrogen-containing atmosphere, subjecting coal powder, coal direct liquefaction circulating oil and coal direct liquefaction catalyst to a coal direct liquefaction reaction to obtain coal direct liquefaction crude oil; step S22, subjecting the coal direct liquefaction crude oil to hydrogenation stabilization to obtain a hydrogenation stabilized product; step S23, subjecting the hydrogenation stabilized product to a first fractionation to obtain a first fraction; step S24, subjecting the first fraction to sequentially hydrogenation refining and hydrocracking to obtain a hydrocracking product; step S25, subjecting the hydrocracking product to a second fractionation to obtain coal direct liquefaction naphtha.

[0014] Further, in step S21, the conditions for the direct coal liquefaction reaction are: reaction temperature of 365-460°C, reaction pressure of 10-22MPa; and / or in step S22, the conditions for hydrogenation stability are: reaction temperature of 320-400°C, preferably 350-380°C; reaction pressure of 8-20MPa, preferably 10-15MPa; hydrogen-to-oil ratio of 300-1000, volume space velocity of 0.5-2.0h -1 ; and / or in step S23, the conditions for the first fractionation are: reaction temperature of 300-350°C, reaction pressure of 0.2-0.8MPa; and / or in step S24, the conditions for hydrofining are: reaction temperature of 260-360°C, preferably 290-340°C; and / or reaction pressure of 2-9MPa, preferably 3-6MPa; and / or volume space velocity of 0.5-3h -1 , preferably 1 to 2 hours -1 ; and / or the hydrogen-to-oil ratio is 200-600, preferably 200-500; and / or in step S24, the conditions for hydrocracking are: reaction temperature is 310-400°C, preferably 325-380°C; reaction pressure is 2-9MPa, preferably 3-7MPa; volume space velocity is 0.5-4h -1 , preferably 1 to 2.5 hours -1 ; The hydrogen-to-oil ratio is 200-800, preferably 300-600; and / or in step S25, the conditions for the second fractionation are: a tower bottom temperature of 290-350°C, preferably 300-330°C; and / or a tower top temperature of 100-150°C, preferably 100-130°C; and / or a tower bottom pressure of 0.1-1.1 MPa, preferably 0.2-0.6 MPa.

[0015] Further, in step S21, the direct coal liquefaction catalyst includes one or more of Fe, Co, Ni, Mo, W, Ti and Ga, preferably including Fe and / or Co; and / or in step S22, the hydrogenation-stable catalyst includes a first carrier and a first active metal component loaded on the first carrier; the first carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the first active metal component includes one or more of Group VIB metals and Group VIII metals, preferably including one or more of Mo, W, Co and Ni; and / or in step S24, the hydrorefined catalyst includes a second carrier and a second active metal component loaded on the second carrier; the second carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the second active metal component includes one or more of Co, Pt, Pd, Ni, W and Mo; and / or in step S24, the hydrocracking catalyst includes a third carrier and a third active metal component loaded on the third carrier; the third carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the third active metal component includes one or more of Co, Pt, Pd, Ni, W and Mo.

[0016] According to another aspect of the present invention, there is provided application of the above-mentioned blended gasoline or the blended gasoline prepared by the above-mentioned preparation method in the automotive field.

[0017] By applying the technical scheme of the present invention, the finished blended gasoline is mainly composed of mixed light hydrocarbons with a boiling range of ≤165°C in the MTP by-product mixed aromatics, coal direct liquefaction naphtha and methyl tert-butyl ether, which fully combines the advantages of extremely low colloid and mechanical impurity content, extremely low benzene sulfur and nitrogen content, and high octane number in the mixed light hydrocarbons with a boiling range of ≤165°C in the MTP by-product mixed aromatics, high content of cycloalkanes and aromatics, low content of sulfur, nitrogen and olefins, moderate density and vapor pressure in the coal direct liquefaction naphtha, and high octane number and low volatility of methyl tert-butyl ether, thereby realizing the value-added utilization of MTP by-product mixed aromatics. Moreover, the blended gasoline has less content of colloid and mechanical impurities and low sulfur content, and is a clean fuel oil. When the blended gasoline of the present invention is applied to the automotive field, it can burn fully, release high calorific value, produce less sediment during combustion, and have a low content of sulfide in the tail gas, so as to pollute the environment less. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] The drawings constituting a part of the present application are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0019] Figure 1 The schematic diagram of the process flow of preparing blended gasoline according to Example 1 of the present invention is shown;

[0020] The above drawings include the following reference numerals:

[0021] 1. Distillation tower; 2. Coal direct liquefaction reactor; 3. Hydrogenation stabilization reactor; 4. First fractionation tower; 5. Hydrofining reactor; 6. Hydrocracking reactor; 7. Second fractionation tower; 8. Stirring tank;

[0022] A. MTP by-product mixed aromatics; B. Mixed light hydrocarbons; C. Heavy components at the bottom of the distillation tower; D. Hydrogen-containing atmosphere; E. Coal powder; F. Coal direct liquefaction circulating oil; G. Coal direct liquefaction crude oil; H. Hydrogenation stable product; I. The first light fraction; K. Hydrogenation refined product; L. Hydrocracking product; M. Coal direct liquefaction naphtha; N. The second heavy fraction; O. Methyl tert-butyl ether; P. Blending gasoline. DETAILED DESCRIPTION

[0023] It should be noted that, in the absence of conflict, the embodiments and features in the embodiments of the present application can be combined with each other. The present invention will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0024] Terminology explanation:

[0025] MTP by-product mixed aromatics: refers to the mixed aromatics produced as a by-product of the methanol to propylene process, whose main components are alkanes, cycloalkanes, olefins and aromatics, and also include some inevitable colloids and mechanical impurities.

[0026] Gel: refers to a macromolecular non-hydrocarbon compound in petroleum whose relative molecular mass and polarity are second only to asphaltene. Its relative density is generally around 1.0. It usually appears as a brown to dark brown viscous liquid with poor fluidity or an amorphous solid.

[0027] Mechanical impurities: Precipitates or suspended matter in petroleum or petroleum products that are insoluble in oil or specified solvents, such as mud, dust, iron filings, fibers and certain insoluble salts.

[0028] As described in the background of the present invention, the prior art has the problem that the MTP by-product mixed aromatics have poor performance and low added value. In order to solve the above problems, in a typical embodiment of the present invention, a blended gasoline is provided, which comprises 40-60% of mixed light hydrocarbons, 25-40% of coal direct liquefaction naphtha and 8-22% of methyl tert-butyl ether by weight percentage; wherein the mixed light hydrocarbons are fraction hydrocarbons obtained by distillation of the MTP by-product mixed aromatics, and the distillation range of the mixed light hydrocarbons is ≤165°C.

[0029] The inventors unexpectedly found that the MTP by-product mixed aromatic hydrocarbons have extremely low benzene sulfur and nitrogen contents and high octane numbers, but high colloid and mechanical impurity contents, as well as high diolefin contents. However, the fraction hydrocarbons with a distillation range of ≤165°C prepared by distillation of the MTP by-product mixed aromatic hydrocarbons are mainly mixed light hydrocarbons, and the contents of colloid and mechanical impurities in the mixed light hydrocarbons are extremely low. The high-boiling point, long-carbon-chain diesel fraction is separated and removed, and has the advantages of being clean and having high combustion efficiency. When it is used as a component for blending gasoline, the gasoline has the advantages of low pollutant emissions, good stability and oxidation stability.

[0030] The coal direct liquefaction naphtha component has high contents of cycloalkanes and aromatics, low sulfur content, low nitrogen content, and low olefin content. In addition, it has moderate density and vapor pressure. When it is used as a gasoline blending component, it can improve the combustion efficiency and lubrication performance of the blended gasoline, and reduce the generation of pollutants such as sulfides and nitrogen compounds after the combustion of the blended gasoline.

[0031] Methyl tert-butyl ether has a high octane number (octane number is 117), low volatility, and stable chemical properties. When used as a gasoline blending component, it can improve the octane number and combustion efficiency of gasoline, and can improve the anti-knock performance of gasoline. In addition, methyl tert-butyl ether can also reduce the volatility of gasoline, thereby helping to reduce the emission of volatile organic compounds and reduce the degree of air pollution.

[0032] The present invention controls the contents of mixed light hydrocarbons with a distillation range of ≤165°C, coal direct liquefaction naphtha and methyl tert-butyl ether prepared by distillation of MTP by-product mixed aromatic hydrocarbons within the above conditions, and the blended gasoline has the characteristics of low sulfur content, high content of cycloalkane and aromatic hydrocarbons and high stability, and is a clean fuel.

[0033] If the content of mixed light hydrocarbons is greater than 60%, the olefin content and gum content of the obtained blended gasoline may exceed the standard. If the content of mixed light hydrocarbons is less than 40%, the vapor pressure and octane number of the obtained blended gasoline may be low and fail to meet the standard requirements. If the content of coal direct liquefaction naphtha is greater than 40%, the vapor pressure and octane number of the obtained blended gasoline may be low and fail to meet the standard requirements. If the content of coal direct liquefaction naphtha is less than 25%, the olefin content and gum content of the obtained blended gasoline may exceed the standard. If the content of methyl tert-butyl ether is greater than 22%, the oxide content of the obtained blended gasoline may exceed the standard. If the content of methyl tert-butyl ether is less than 8%, the octane number and vapor pressure of the obtained blended gasoline may fail to meet the standard requirements.

[0034] The present invention is the first to prepare the mixed light hydrocarbons with a boiling range of ≤165°C by distilling the MTP byproduct mixed aromatic hydrocarbons, blending them with coal direct liquefaction naphtha and methyl tert-butyl ether to form blended gasoline, which fully combines the advantages of extremely low colloid and mechanical impurity content, extremely low benzene sulfur and nitrogen content, and high octane number in the mixed light hydrocarbons, high cycloalkane and aromatic content, low sulfur nitrogen olefin content, moderate density and vapor pressure of coal direct liquefaction naphtha, and high octane number and low volatility of methyl tert-butyl ether, and can improve the value-added utilization and safety performance of mixed aromatic hydrocarbons, thereby effectively improving the quality and efficiency of mixed aromatic hydrocarbons, and can make comprehensive use of coal direct liquefaction naphtha, thereby reducing the cost of gasoline. In addition, the content of colloid, mechanical impurities, sulfide, etc. in the obtained finished gasoline is extremely low, which helps to reduce pollution to the environment and is a clean fuel.

[0035] In a preferred embodiment, the mixed light hydrocarbons include 30 to 51 parts of olefins, 10 to 30 parts of aromatics, 8 to 25 parts of cycloalkanes, 4 to 10 parts of normal alkanes, 18 to 38 parts of isoalkanes, 0 to 0.01 parts of mechanical impurities and colloids, and the mass concentration of colloids is less than 80 mg / 100 mL; wherein the olefins include monoolefins and diolefins, and the weight ratio of the two is (96.7 to 100): (0 to 3.3). Under the above conditions, the content of colloids and mechanical impurities in the mixed light hydrocarbons is lower, and the content of diolefin components is lower. When used as a blending gasoline component, the blending gasoline has better stability and oxidation stability.

[0036] In order to further improve the anti-knock performance of blended gasoline and make more full use of the chemical product coal direct liquefaction naphtha, in a preferred embodiment, the blended gasoline includes, by weight percentage: 45-55% mixed light hydrocarbons, 30-40% coal direct liquefaction naphtha and 10-20% methyl tert-butyl ether. Under the above conditions, coal direct liquefaction naphtha can be more fully utilized, which is more conducive to reducing the preparation cost of blended gasoline. In addition, the blended gasoline has a higher content of cycloalkanes and aromatics, and at the same time, the sulfur content, nitrogen content, and olefin content are lower, and the added value is higher.

[0037] In order to further improve the anti-knock performance of coal direct liquefaction naphtha, in a preferred embodiment, the coal direct liquefaction naphtha includes 50 to 70 parts of cycloalkanes, 14 to 18 parts of aromatics, 10 to 20 parts of paraffins, and 10 to 15 parts of olefins by weight. Under the above conditions, the content of cycloalkanes and aromatics in the coal direct liquefaction naphtha is higher, the anti-knock performance of the coal direct liquefaction naphtha is better, and the cost of preparing blended gasoline is lower.

[0038] In another typical embodiment of the present invention, a method for preparing the above-mentioned blended gasoline is also provided, comprising the following steps: step S1, distilling the MTP by-product mixed aromatic hydrocarbons to obtain mixed light hydrocarbons, wherein the distillation range of the mixed light hydrocarbons is ≤165°C; step S2, mixing coal direct liquefaction naphtha, methyl tert-butyl ether and the mixed light hydrocarbons to obtain blended gasoline.

[0039] Compared with the existing mixed aromatics reforming technology, the process of the present invention is simple, the equipment and material costs are low, the obtained product has high added value and significant economic benefits. In addition, the use of mixed aromatics, a byproduct of methanol to propylene, instead of petroleum-based products to prepare blended gasoline has a certain role in alleviating the energy crisis.

[0040] In a preferred embodiment, the MTP by-product mixed aromatics include 20 to 46.5 parts of olefins, 20 to 60 parts of aromatics, 6 to 15 parts of cycloalkanes, 2 to 5 parts of normal alkanes, 18 to 35 parts of isoalkanes, 0.01 to 0.5 parts of mechanical impurities and the remainder of colloid, and the mass concentration of the colloid is 110 to 220 mg / 100 mL; wherein the olefins include monoolefins and diolefins, and the weight ratio of the two is (92.5 to 99.957): (0.043 to 7.5). Under the above conditions, the aromatic content in the MTP by-product mixed aromatics is higher, and the anti-knock performance of the prepared blended gasoline is better and the added value is higher.

[0041] In order to further reduce the content of colloid and asphaltene components in the MTP by-product mixed aromatics, thereby further improving the stability of the blended gasoline, in a preferred embodiment, the distillation is carried out in a distillation tower, the number of theoretical plates of the distillation tower is 15 to 30, the reflux ratio is (1 to 10): 1, the extraction rate is 10 to 20 mL / min, the heating rate is 0.5 to 8 ° C / min, and the tower top pressure is 0.1 to 0.5 MPa. Under the above conditions, the heavy components of colloid and asphaltene in the MTP by-product mixed aromatics are fully removed, and the mixed light hydrocarbons have more stable characteristics.

[0042] In order to make the coal direct liquefaction naphtha, methyl tert-butyl ether and mixed light hydrocarbons more uniformly mixed, so as to make the anti-knock performance and oxidation stability of the blended gasoline more stable, in a preferred embodiment, in step S2, the mixing method includes one or more of mechanical stirring, compressed air stirring, pump circulation and pipeline blending; preferably, the speed of mechanical stirring is 500-600rpm; and / or the time is 30-40 minutes. In a preferred embodiment, the first mixing equipment is an antistatic enamel stirring kettle, under which conditions, the mixing is more uniform.

[0043] In order to make the CDL naphtha have more aromatic components and higher yield, in a preferred embodiment, step S2 also includes the following steps: step S21, in a hydrogen-containing atmosphere, the coal powder, the CDL circulating oil and the CDL catalyst are subjected to a CDL liquefaction reaction to obtain CDL crude oil; step S22, the CDL crude oil is subjected to hydrogenation stabilization to obtain a hydrogenation stabilized product; step S23, the hydrogenation stabilized product is subjected to a first fractionation to obtain a first fraction; step S24, the first fraction is subjected to hydrogenation refining and hydrocracking in sequence to obtain a hydrocracking product; step S25, the hydrocracking product is subjected to a second fractionation to obtain CDL naphtha. Under the above conditions, with coal as the raw material, after direct coal liquefaction, hydrogenation stabilization, hydrogenation refining, hydrocracking and fractionation, the CDL naphtha obtained has less sulfur, nitrogen and olefin content, which is more conducive to the preparation of environmentally friendly and clean blended gasoline.

[0044] In order to further improve the yield of coal direct liquefaction naphtha and further improve its preparation efficiency, in a preferred embodiment, in step S21, the conditions for the coal direct liquefaction reaction are: the reaction temperature is 365-460°C, and the reaction pressure is 10-22MPa; and / or the second mixing method includes one or more of mechanical stirring, compressed air stirring, pump circulation and pipeline blending; and / or in step S22, the conditions for hydrogenation stability are: the reaction temperature is 320-400°C, preferably 350-380°C; the reaction pressure is 8-20MPa, preferably 10-15MPa; the hydrogen-oil ratio is 300-1000, and the volume space velocity is 0.5-2.0h -1 ; and / or in step S23, the conditions for the first fractionation are: reaction temperature of 300-350°C, reaction pressure of 0.2-0.8MPa; and / or in step S24, the conditions for hydrofining are: reaction temperature of 260-360°C, preferably 290-340°C; and / or reaction pressure of 2-9MPa, preferably 3-6MPa; and / or volume space velocity of 0.5-3h -1 , preferably 1 to 2 hours -1 ; and / or the hydrogen-to-oil ratio is 200-600, preferably 200-500; and / or in step S24, the conditions for hydrocracking are: reaction temperature is 310-400°C, preferably 325-380°C; reaction pressure is 2-9MPa, preferably 3-7MPa; volume space velocity is 0.5-4h -1 , preferably 1 to 2.5 hours -1; hydrogen-to-oil ratio is 200-800, preferably 300-600; and / or in step S25, the conditions for the second fractionation are: tower bottom temperature 290-350°C, preferably 300-330°C; and / or tower top temperature 100-150°C, preferably 100-130°C; and / or tower bottom pressure 0.1-1.1MPa, preferably 0.2-0.6MPa. Under the above conditions, the coal direct liquefaction naphtha yield is higher and the aromatics content is higher.

[0045] In order to further improve the activity of coal direct liquefaction, hydrogenation stabilization, hydrorefining, and hydrocracking reaction catalysts and the selectivity for target products, thereby further improving the yield of coal direct liquefaction naphtha, in a preferred embodiment, in step S21, the coal direct liquefaction catalyst includes one or more of Fe, Co, Ni, Mo, W, Ti and Ga, preferably Fe and / or Co; and / or in step S22, the hydrogenation stabilization catalyst includes a first carrier and a first active metal component supported on the first carrier; the first carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the first active metal component includes one or more of Group VIB metals and Group VIII metals species, preferably including one or more of Mo, W, Co and Ni; and / or in step S24, the hydrorefining catalyst includes a second carrier and a second active metal component supported on the second carrier; the second carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the second active metal component includes one or more of Co, Pt, Pd, Ni, W and Mo; and / or in step S24, the hydrocracking catalyst includes a third carrier and a third active metal component supported on the third carrier; the third carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the third active metal component includes one or more of Co, Pt, Pd, Ni, W and Mo.

[0046] In another typical embodiment of the present invention, there is also provided an application of the above blended gasoline or the blended gasoline prepared by the above preparation method in the automotive field. When the above blended gasoline or the blended gasoline prepared by the above preparation method of blended gasoline is applied to the automotive field, it can burn fully, release high calorific value, produce less sediment during combustion, and has a low content of sulfide in the exhaust gas, thereby causing less pollution to the environment.

[0047] Typically but not limiting, by weight percentage, in the blended gasoline, mixed light hydrocarbons account for 40%, 45%, 50%, 55%, 60% or a range consisting of any two of them, coal direct liquefaction naphtha accounts for 25%, 30%, 35%, 40% or a range consisting of any two of them, and methyl tert-butyl ether accounts for 8%, 10%, 15%, 20%, 22% or a range consisting of any two of them.

[0048] Typically but not limiting, in blended gasoline, the distillation range of mixed light hydrocarbons is 160°C, 161°C, 162°C, 163°C, 164°C, 165°C or a range consisting of any two of them.

[0049] The present application is further described in detail below in conjunction with specific embodiments. These embodiments should not be construed as limiting the scope of protection claimed in the present application.

[0050] Example 1

[0051] The schematic diagram of the preparation process of blended gasoline is shown in Figure 1 .

[0052] In parts by weight, the MTP by-product mixed aromatic hydrocarbons include 32 parts of olefins, 40 parts of aromatics, 10 parts of cycloalkanes, 3 parts of normal alkanes, 26 parts of isoalkanes, 0.25 parts of mechanical impurities and the remainder of the first colloid, and the mass concentration of the first colloid is 170 mg / 100 mL; among which, the weight ratio of monoolefins and diolefins in the olefins is 96.2:3.8.

[0053] Step S1, sending the MTP by-product mixed aromatic hydrocarbons A into the distillation tower 1 for distillation, the theoretical number of plates of the distillation tower is 22, the reflux ratio is 5:1, the extraction rate is 15mL / min, the heating rate is 4℃ / min, the tower top pressure is 0.3MPa, and mixed light hydrocarbons B (distillation range is 42-165℃) are obtained at the tower top. By weight, the mixed light hydrocarbons include: 40 parts of olefins, 20 parts of aromatics, 15 parts of cycloalkanes, 6 parts of normal alkanes, 28 parts of isoalkanes, 0.005 parts of mechanical impurities and the remainder of the second colloid, and the mass concentration of the second colloid is 45mg / 100mL; wherein, the weight ratio of monoolefins to diolefins in the olefins is 98.4:1.6. A heavy component C (mainly a diesel component) at the bottom of the distillation tower with a distillation range of 165-240℃ is obtained at the bottom of the tower, and the heavy component is sent for refining and blending to prepare a qualified diesel product.

[0054] Step S2, in the coal direct liquefaction reactor 2, the coal powder E, the coal direct liquefaction circulating oil F and the coal direct liquefaction catalyst (Fe) are subjected to a coal direct liquefaction reaction at a reaction temperature of 400°C and a reaction pressure of 16MPa to obtain the coal direct liquefaction crude oil G. The coal direct liquefaction crude oil G is sent to the hydrogenation stabilization reactor 3, and the reaction temperature is 365°C, the reaction pressure is 12MPa, the hydrogen-to-oil ratio is 600, and the volume space velocity is 1.2h -1, and the catalyst is Mo-loaded alumina to obtain a hydrogenated stabilized product H. The hydrogenated stabilized product H is sent to the first fractionation tower 4, and the first fractionation is carried out under the conditions of a reaction temperature of 325°C and a reaction pressure of 0.6MPa, and the first light fraction I is obtained at the top of the tower. The first light fraction I is sent to the hydrofining reactor 5, and the reaction temperature is 315°C, the reaction pressure is 4.5MPa, and the volume space velocity is 1.5h -1 , a hydrogen-to-oil ratio of 350, and a catalyst of Mo-Ni-loaded alumina, to obtain a hydrorefining product K. The hydrorefining product K was fed into a hydrocracking reactor 6 and heated at a reaction temperature of 350°C, a reaction pressure of 5 MPa, and a volume space velocity of 2 h -1 , a hydrogen-to-oil ratio of 450, and a catalyst of alumina loaded with Mo-Ni-W to obtain a hydrocracking product L. The hydrocracking product is sent to a second fractionation tower 7, with a bottom temperature of 315°C, a top temperature of 115°C, and a bottom pressure of 0.4MPa, for a second fractionation, and a second heavy fraction N (mainly composed of cycloalkanes) with a distillation range of 160-350°C is obtained at the bottom of the tower, and the heavy fraction is sent for blending to prepare a diesel product; a coal direct liquefaction naphtha M with a distillation range of 45-166°C is obtained at the top of the tower, and the coal direct liquefaction naphtha includes 60 parts of cycloalkanes, 16 parts of aromatics, 15 parts of paraffins, and 12 parts of olefins by weight.

[0055] Step S3, by weight percentage, 50% of mixed light hydrocarbons, 35% of coal direct liquefaction naphtha and 15% of methyl tert-butyl ether O are fed into a stirring kettle 8 (antistatic enamel high-speed stirring kettle), and mixed under normal pressure, normal temperature, a rotation speed of 550 rpm, and a time of 35 minutes to obtain blended gasoline P. The prepared blended gasoline is used in the automotive field.

[0056] The test results of the physical and chemical properties of MTP by-products, such as mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether, are shown in Table 1.

[0057] Example 2

[0058] The only difference from Example 1 is:

[0059] In terms of weight percentage, the blended gasoline includes 40% mixed light hydrocarbons, 40% coal direct liquefaction naphtha and 20% methyl tert-butyl ether.

[0060] The test results of the physical and chemical properties of MTP by-products, such as mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether, are shown in Table 1.

[0061] Example 3

[0062] The only difference from Example 1 is:

[0063] In terms of weight percentage, the blended gasoline includes 60% mixed light hydrocarbons, 25% coal direct liquefaction naphtha and 15% methyl tert-butyl ether.

[0064] The test results of the physical and chemical properties of MTP by-products, such as mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether, are shown in Table 1.

[0065] Example 4

[0066] The only difference from Example 1 is:

[0067] In terms of weight percentage, the blended gasoline includes 45% mixed light hydrocarbons, 35% coal direct liquefaction naphtha and 20% methyl tert-butyl ether.

[0068] The test results of the physical and chemical properties of MTP by-products, such as mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether, are shown in Table 1.

[0069] Example 5

[0070] The only difference from Example 1 is:

[0071] In terms of weight percentage, the blended gasoline includes 55% mixed light hydrocarbons, 35% coal direct liquefaction naphtha and 10% methyl tert-butyl ether.

[0072] The test results of the physical and chemical properties of MTP by-products, such as mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether, are shown in Table 1.

[0073] Example 6

[0074] The only difference from Example 1 is:

[0075] In parts by weight, the MTP by-product mixed aromatic hydrocarbons include 20 parts of olefins, 52 parts of aromatic hydrocarbons, 6 parts of cycloalkanes, 5 parts of normal alkanes, 18 parts of isoalkanes, 0.01 parts of mechanical impurities and the remainder of the first colloid, and the mass concentration of the first colloid is 110 mg / 100 mL; wherein the weight ratio of monoolefins and diolefins in the olefins is 92.5:7.5.

[0076] The mixed light hydrocarbons include, by weight: 35 parts of olefins, 25 parts of aromatics, 11 parts of cycloalkanes, 9 parts of normal alkanes, 33 parts of isoalkanes, 0.002 parts of mechanical impurities and the remainder of a second colloid, wherein the mass concentration of the second colloid is 50 mg / 100 mL; wherein the weight ratio of monoolefins to diolefins in the olefins is 97:3.

[0077] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 2.

[0078] Example 7

[0079] The only difference from Example 1 is:

[0080] In parts by weight, the MTP by-product mixed aromatic hydrocarbons include 46.5 parts of olefins, 20 parts of aromatic hydrocarbons, 15 parts of cycloalkanes, 2 parts of normal alkanes, 35 parts of isoalkanes, 0.5 parts of mechanical impurities and the remainder of the first colloid, and the mass concentration of the first colloid is 220 mg / 100 mL; wherein, the weight ratio of monoolefins and diolefins in the olefins is 99.957:0.043.

[0081] The mixed light hydrocarbons include, by weight, 48 parts of olefins, 15 parts of aromatics, 9 parts of cycloalkanes, 5 parts of normal alkanes, 20 parts of isoalkanes, 0.003 parts of mechanical impurities and the remainder of a second colloid, wherein the mass concentration of the second colloid is 48 mg / 100 mL; wherein the weight ratio of monoolefins to diolefins in the olefins is 97.5:2.5.

[0082] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 2.

[0083] Example 8

[0084] The only difference from Example 1 is:

[0085] In parts by weight, the MTP by-product mixed aromatic hydrocarbons include 25 parts of olefins, 55 parts of aromatic hydrocarbons, 9 parts of cycloalkanes, 4.5 parts of normal alkanes, 22 parts of isoalkanes, 0.1 parts of mechanical impurities and the remainder of the first colloid, and the mass concentration of the first colloid is 130 mg / 100 mL; wherein the weight ratio of monoolefins and diolefins in the olefins is 99.957:0.043.

[0086] The mixed light hydrocarbons include, by weight: 30 parts of olefins, 30 parts of aromatics, 8 parts of cycloalkanes, 10 parts of normal alkanes, 18 parts of isoalkanes, 0.001 parts of mechanical impurities and the remainder of a second colloid, wherein the mass concentration of the second colloid is 20 mg / 100 mL; wherein the weight ratio of monoolefins to diolefins in the olefins is 99.9:0.1.

[0087] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 3.

[0088] Example 9

[0089] The only difference from Example 1 is:

[0090] In parts by weight, the MTP by-product mixed aromatic hydrocarbons include 44 parts of olefins, 25 parts of aromatic hydrocarbons, 13 parts of cycloalkanes, 4 parts of normal alkanes, 30 parts of isoalkanes, 0.4 parts of mechanical impurities and the remainder of the first colloid, and the mass concentration of the first colloid is 200 mg / 100 mL; wherein the weight ratio of monoolefins and diolefins in the olefins is 92.5:7.5.

[0091] The mixed light hydrocarbons include, by weight, 51 parts of olefins, 10 parts of aromatics, 25 parts of cycloalkanes, 4 parts of normal alkanes, 38 parts of isoalkanes, 0.01 parts of mechanical impurities and the remainder of a second colloid, wherein the mass concentration of the second colloid is 60 mg / 100 mL; wherein the weight ratio of monoolefins to diolefins in the olefins is 96.7:3.3.

[0092] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 3.

[0093] Example 10

[0094] The only difference from Example 1 is:

[0095] The theoretical number of plates of the distillation tower is 30, the reflux ratio is 1:1, the production rate is 10 mL / min, the heating rate is 8 ° C / min, the top pressure is 0.1 MPa, and mixed light hydrocarbons with a distillation range of 43 to 166 ° C are obtained at the top of the distillation tower.

[0096] The mixed light hydrocarbons include, by weight, 42 parts of olefins, 18 parts of aromatics, 17 parts of cycloalkanes, 8 parts of normal alkanes, 25 parts of isoalkanes, 0.008 parts of mechanical impurities and the remainder of a second colloid, wherein the mass concentration of the second colloid is 70 mg / 100 mL; wherein the weight ratio of monoolefins to diolefins in the olefins is 98:2; a heavy component (mainly a diesel component) at the bottom of the distillation tower with a distillation range of 166 to 240° C. is obtained at the bottom of the tower, and the heavy component is sent for refining and blending to prepare a qualified diesel product.

[0097] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 4.

[0098] Embodiment 11

[0099] The only difference from Example 1 is:

[0100] The theoretical number of plates of the distillation tower is 15, the reflux ratio is 10:1, the production rate is 20 mL / min, the heating rate is 0.5 °C / min, the top pressure is 0.5 MPa, and mixed light hydrocarbons with a distillation range of 45 to 160 °C are obtained at the top of the distillation tower.

[0101] The mixed light hydrocarbons include, by weight, 39 parts of olefins, 20 parts of aromatics, 18 parts of cycloalkanes, 9 parts of normal alkanes, 27 parts of isoalkanes, 0.006 parts of mechanical impurities and the remainder of a second colloid, wherein the mass concentration of the second colloid is 60 mg / 100 mL; wherein the weight ratio of monoolefins to diolefins in the olefins is 98.7:1.3; a heavy component (mainly a diesel component) at the bottom of the distillation tower with a distillation range of 160 to 240° C. is obtained at the bottom of the tower, and the heavy component is sent for refining and blending to prepare a qualified diesel product.

[0102] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 4.

[0103] Example 12

[0104] The only difference from Example 1 is:

[0105] Step S3, according to the weight percentage, 50% of mixed light hydrocarbons, 35% of coal direct liquefaction naphtha and 15% of methyl tert-butyl ether are fed into a stirring tank (mechanical stirring tank), and mixed at a speed of 500 rpm for 40 minutes to obtain blended gasoline.

[0106] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 5.

[0107] Example 13

[0108] The only difference from Example 1 is:

[0109] Step S3, according to the weight percentage, 50% of mixed light hydrocarbons, 35% of coal direct liquefaction naphtha and 15% of methyl tert-butyl ether are fed into a stirring tank (mechanical stirring tank), and mixed at a speed of 600 rpm for 30 minutes to obtain blended gasoline.

[0110] The test results of the physical and chemical properties of MTP by-products mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 5.

[0111] Embodiment 14

[0112] The only difference from Example 1 is:

[0113] Step S2, the conditions for the direct coal liquefaction reaction are a reaction temperature of 365°C, a reaction pressure of 22 MPa, and a catalyst of Co;

[0114] The stable conditions for hydrogenation are reaction temperature of 350°C, reaction pressure of 15 MPa, hydrogen-to-oil ratio of 300, and volume space velocity of 2 h -1, the catalyst is silicon oxide loaded with Mo;

[0115] The conditions of the first fractionation are reaction temperature of 300°C and reaction pressure of 0.8MPa; a first light fraction I is obtained at the top of the first fractionation tower;

[0116] The conditions for hydrotreating are reaction temperature of 290°C, reaction pressure of 6 MPa, and volume space velocity of 1 h -1 , hydrogen-to-oil ratio is 500, and the catalyst is Co-loaded silicon oxide;

[0117] The hydrocracking conditions are as follows: reaction temperature of 325°C, reaction pressure of 7 MPa, volume space velocity of 1 h -1 , hydrogen-to-oil ratio is 600, and the catalyst is Co-loaded silica;

[0118] The bottom temperature of the second distillation tower is 300°C, the top temperature is 130°C, and the bottom pressure is 0.2MPa. A second heavy fraction (mainly composed of cycloalkanes) with a distillation range of 165-350°C is obtained at the bottom of the second distillation tower, and coal direct liquefaction naphtha with a distillation range of 45-165°C is obtained at the top. By weight, the coal direct liquefaction naphtha includes 58 parts of cycloalkanes, 18 parts of aromatics, 16 parts of chain alkanes, and 11 parts of olefins.

[0119] The test results of the physical and chemical properties of MTP by-product mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 6.

[0120] Embodiment 15

[0121] The only difference from Example 1 is:

[0122] Step S2, the conditions for the direct coal liquefaction reaction are a reaction temperature of 460°C, a reaction pressure of 10 MPa, and catalysts of Fe and Co;

[0123] The stable conditions for hydrogenation are reaction temperature of 380°C, reaction pressure of 10 MPa, hydrogen-to-oil ratio of 1000, and volume space velocity of 0.5 h -1 , the catalyst is Ni-loaded titanium oxide;

[0124] The conditions for the first fractionation are a reaction temperature of 350°C and a reaction pressure of 0.2 MPa; a first light fraction I is obtained at the top of the first fractionation tower;

[0125] The conditions for hydrotreating are reaction temperature of 340°C, reaction pressure of 3 MPa, and volume space velocity of 2 h -1 , the hydrogen-to-oil ratio is 200, and the catalyst is Pt-loaded titanium oxide;

[0126] The hydrocracking conditions were as follows: reaction temperature of 380°C, reaction pressure of 3 MPa, volume space velocity of 2.5 h-1 , the hydrogen-to-oil ratio is 300, and the catalyst is Pt-loaded titanium oxide;

[0127] The bottom temperature of the second distillation tower is 330°C, the top temperature is 100°C, and the bottom pressure is 0.6MPa. A second heavy fraction (mainly composed of cycloalkanes) with a distillation range of 165-355°C is obtained at the bottom of the second distillation tower, and coal direct liquefaction naphtha with a distillation range of 40-165°C is obtained at the top. By weight, the coal direct liquefaction naphtha includes 60 parts of cycloalkanes, 18 parts of aromatics, 17 parts of chain alkanes, and 11 parts of olefins.

[0128] The test results of the physical and chemical properties of MTP by-product mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 6.

[0129] Example 16

[0130] The only difference from Example 1 is:

[0131] Step S2, the conditions for the direct coal liquefaction reaction are a reaction temperature of 365°C, a reaction pressure of 22MPa, and a catalyst of tungsten;

[0132] The stable conditions for hydrogenation are reaction temperature of 320°C, reaction pressure of 20 MPa, hydrogen-to-oil ratio of 300, and volume space velocity of 2 h -1 , the catalyst is alumina loaded with Mo;

[0133] The conditions for the first fractionation are a reaction temperature of 300°C and a reaction pressure of 0.8 MPa; a first light fraction is obtained at the top of the first fractionation tower;

[0134] The conditions for hydrotreating are reaction temperature of 260°C, reaction pressure of 9 MPa, and volume space velocity of 0.5 h -1 , hydrogen-oil ratio is 600, catalyst is Mo-Ni loaded silicon oxide;

[0135] The hydrocracking conditions were as follows: reaction temperature of 310°C, reaction pressure of 9 MPa, volume space velocity of 0.5 h -1 , hydrogen-to-oil ratio is 800, and the catalyst is Mo-Ni-W-loaded silicon oxide;

[0136] The bottom temperature of the second distillation tower is 290°C, the top temperature is 150°C, and the bottom pressure is 0.1MPa. A second heavy fraction (mainly composed of cycloalkanes) with a distillation range of 160-355°C is obtained at the bottom of the second distillation tower, and coal direct liquefaction naphtha with a distillation range of 40-160°C is obtained at the top. By weight, the coal direct liquefaction naphtha includes 60 parts of cycloalkanes, 19 parts of aromatics, 17 parts of chain alkanes, and 12 parts of olefins.

[0137] The test results of the physical and chemical properties of MTP by-product mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 7.

[0138] Embodiment 17

[0139] The only difference from Example 1 is:

[0140] Step S2, the conditions for the direct coal liquefaction reaction are a reaction temperature of 460°C, a reaction pressure of 10 MPa, and a catalyst of Ti;

[0141] The stable conditions for hydrogenation are reaction temperature of 400°C, reaction pressure of 8 MPa, hydrogen-to-oil ratio of 1000, and volume space velocity of 0.5 h -1 , the catalyst is Ni-loaded alumina;

[0142] The conditions for the first fractionation are a reaction temperature of 350°C and a reaction pressure of 0.2 MPa; a first light fraction is obtained at the top of the first fractionation tower;

[0143] The conditions for hydrotreating are reaction temperature of 360°C, reaction pressure of 2 MPa, and volume space velocity of 3 h -1 , the hydrogen-oil ratio is 200, and the catalyst is Mo-Ni-loaded titanium oxide;

[0144] The conditions for hydrocracking are a reaction temperature of 400°C, a reaction pressure of 2 MPa, and a volume space velocity of 4 h -1 , the hydrogen-to-oil ratio is 200, and the catalyst is titanium oxide loaded with Mo-Ni-W;

[0145] The bottom temperature of the second distillation tower is 350°C, the top temperature is 100°C, and the bottom pressure is 1.1MPa. A second heavy fraction (mainly composed of cycloalkanes) with a distillation range of 160-360°C is obtained at the bottom of the second distillation tower, and coal direct liquefaction naphtha with a distillation range of 45-160°C is obtained at the top. By weight, the coal direct liquefaction naphtha includes 60 parts of cycloalkanes, 19 parts of aromatics, 15 parts of paraffins, and 12 parts of olefins.

[0146] The test results of the physical and chemical properties of MTP by-product mixed aromatics, mixed light hydrocarbons, coal direct liquefaction naphtha and methyl tert-butyl ether are shown in Table 7.

[0147] Test method:

[0148] Octane number test: refer to GB / T 5487-2015 for testing. Gel test: refer to GB / T 8019-2008 for testing.

[0149] Table 1

[0150]

[0151] Table 2

[0152]

[0153]

[0154] Table 3

[0155]

[0156]

[0157] Table 4

[0158]

[0159] Table 5

[0160]

[0161]

[0162] Table 6

[0163]

[0164]

[0165] Table 7

[0166]

[0167] As can be seen from the above, the finished blended gasoline of the embodiment of the present invention is mainly composed of mixed light hydrocarbons with a boiling range of ≤165°C in the MTP by-product mixed aromatics, coal direct liquefaction naphtha and methyl tert-butyl ether, which fully combines the advantages of extremely low colloid and mechanical impurity content, extremely low benzene sulfur and nitrogen content, and high octane number in the mixed light hydrocarbons with a boiling range of ≤165°C in the MTP by-product mixed aromatics, high content of cycloalkanes and aromatics, low content of sulfur nitrogen olefins, moderate density and vapor pressure in coal direct liquefaction naphtha, and high octane number and low volatility of methyl tert-butyl ether, realizing the value-added utilization of MTP by-product mixed aromatics. Moreover, the blended gasoline has less colloid and mechanical impurity content and low sulfur content, and is a clean fuel oil. The blended gasoline of the present invention can be fully burned when applied to the automotive field, has a high calorific value released, less sediment produced during combustion, and a low content of sulfides in the tail gas, which pollutes the environment less.

[0168] In addition, it can be seen that when the process parameters are within the preferred range of the present invention, the by-product mixed aromatics of MTP can be fully utilized to increase its added value.

[0169] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A blended gasoline, characterized in that: Calculated by weight percentage, The blended gasoline comprises 40-60% of mixed light hydrocarbons, 25-40% of coal direct liquefaction naphtha and 8-22% of methyl tert-butyl ether; The mixed light hydrocarbons are fraction hydrocarbons obtained by distillation of MTP by-product mixed aromatic hydrocarbons, and the distillation range of the mixed light hydrocarbons is ≤165°C.

2. The blended gasoline according to claim 1, characterized in that: In parts by weight, the mixed light hydrocarbons include 30 to 51 parts of olefins, 10 to 30 parts of aromatics, 8 to 25 parts of cycloalkanes, 4 to 10 parts of normal alkanes, 18 to 38 parts of isoalkanes, 0 to 0.01 parts of mechanical impurities and colloids, and the mass concentration of the colloids is less than 80 mg / 100 mL; The olefins include monoolefins and diolefins, and the weight ratio of the two is (96.7-100):(0-3.3).

3. The blended gasoline according to claim 1 or 2, characterized in that: Measured by weight percentage, the blended gasoline includes: 45-55% of the mixed light hydrocarbons, 30-40% of the coal direct liquefaction naphtha and 10-20% of the methyl tert-butyl ether.

4. The method for preparing the blended gasoline according to any one of claims 1 to 3, characterized in that: The following steps are involved: Step S1, distilling the MTP by-product mixed aromatic hydrocarbons to obtain mixed light hydrocarbons, wherein the distillation range of the mixed light hydrocarbons is ≤165°C; Step S2, mixing coal direct liquefaction naphtha, methyl tert-butyl ether and the mixed light hydrocarbons to obtain the blended gasoline.

5. The preparation method according to claim 4, characterized in that: In the step S1, by weight, The MTP by-product mixed aromatic hydrocarbons include 20 to 46.5 parts of olefins, 20 to 60 parts of aromatic hydrocarbons, 6 to 15 parts of cycloalkanes, 2 to 5 parts of normal alkanes, 18 to 35 parts of isoalkanes, 0.01 to 0.5 parts of mechanical impurities and the remainder of colloid, and the mass concentration of the colloid is 110 to 220 mg / 100 mL; wherein the olefins include monoolefins and diolefins, and the weight ratio of the two is (92.5 to 99.957):(0.043 to 7.5); and / or The distillation is carried out in a distillation tower, the number of theoretical plates of the distillation tower is 15 to 30, the reflux ratio is (1 to 10):1, the extraction rate is 10 to 20 mL / min, the heating rate is 0.5 to 8°C / min, and the tower top pressure is 0.1 to 0.5 MPa.

6. The preparation method according to claim 4 or 5, characterized in that: In step S2, the mixing method includes one or more of mechanical stirring, compressed air stirring, pump circulation and pipeline blending.

7. The preparation method according to any one of claims 4 to 6, characterized in that: The step S2 further comprises the following steps: Step S21, in a hydrogen-containing atmosphere, subjecting pulverized coal, coal direct liquefaction circulating oil and a coal direct liquefaction catalyst to a coal direct liquefaction reaction to obtain coal direct liquefaction crude oil; Step S22, hydrogenating and stabilizing the CDL crude oil to obtain a hydrogenated stabilized product; Step S23, performing a first fractionation on the hydrogenation stabilized product to obtain a first fraction; Step S24, sequentially performing hydrotreating and hydrocracking on the first fraction to obtain a hydrocracking product; Step S25, performing a second fractionation on the hydrocracking product to obtain the coal direct liquefaction naphtha.

8. The preparation method according to claim 7, characterized in that: In step S21, the conditions of the coal direct liquefaction reaction are: reaction temperature of 365-460° C., reaction pressure of 10-22 MPa; and / or In step S22, the stable conditions of hydrogenation are: reaction temperature is 320-400°C, preferably 350-380°C; reaction pressure is 8-20MPa, preferably 10-15MPa; hydrogen-to-oil ratio is 300-1000, and volume space velocity is 0.5-2.0h -1 ; and / or In the step S23, the conditions of the first fractionation are: reaction temperature of 300-350° C., reaction pressure of 0.2-0.8 MPa; and / or In step S24, the conditions for the hydrofining are: the reaction temperature is 260-360°C, preferably 290-340°C; and / or the reaction pressure is 2-9MPa, preferably 3-6MPa; and / or the volume space velocity is 0.5-3h -1 , preferably 1 to 2 hours -1 ; and / or a hydrogen-to-oil ratio of 200 to 600, preferably 200 to 500; and / or In step S24, the conditions for the hydrocracking are: reaction temperature of 310-400°C, preferably 325-380°C; reaction pressure of 2-9MPa, preferably 3-7MPa; volume space velocity of 0.5-4h -1 , preferably 1 to 2.5 hours -1 ; Hydrogen to oil ratio is 200 to 800, preferably 300 to 600; and / or In step S25, the conditions for the second fractionation are: a tower bottom temperature of 290 to 350°C, preferably 300 to 330°C; and / or a tower top temperature of 100 to 150°C, preferably 100 to 130°C; and / or a tower bottom pressure of 0.1 to 1.1 MPa, preferably 0.2 to 0.6 MPa.

9. The preparation method according to claim 7 or 8, characterized in that: In step S21, the coal direct liquefaction catalyst includes one or more of Fe, Co, Ni, Mo, W, Ti and Ga, preferably includes Fe and / or Co; and / or In step S22, the hydrogenation-stable catalyst comprises a first carrier and a first active metal component supported on the first carrier; the first carrier comprises one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the first active metal component comprises one or more of Group VIB metals and Group VIII metals, preferably one or more of Mo, W, Co and Ni; and / or In step S24, the hydrorefining catalyst includes a second carrier and a second active metal component supported on the second carrier; the second carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the second active metal component includes one or more of Co, Pt, Pd, Ni, W and Mo; and / or In step S24, the hydrocracking catalyst includes a third carrier and a third active metal component supported on the third carrier; the third carrier includes one or more of silicon oxide, aluminum oxide and titanium oxide; and / or the third active metal component includes one or more of Co, Pt, Pd, Ni, W and Mo.

10. Use of the blended gasoline according to any one of claims 1 to 3 or the blended gasoline prepared by the preparation method according to any one of claims 4 to 9 in the automotive field.

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