A jet fuel composition and preparation method thereof

Abstract

The present invention relates to a jet fuel composition and a preparation method thereof. The jet fuel composition comprises 5-20% by mass of C 9‑18 alkanes, 75-95% by mass of C 9‑18 cycloalkanes, and ≤7% by mass of C 9‑18 aromatics. The jet fuel composition has low sulfur, nitrogen, and aromatic hydrocarbon contents and is a clean jet fuel composition. In the preparation method provided by the present invention, the catalytic cracking light cycle oil is subjected to hydrotreating and then hydrodearomatization, and the reaction product is subjected to gas-liquid separation and fractionation to obtain the jet fuel composition. The present invention can obtain high-density jet fuel components at a relatively low operating pressure and a relatively low reaction temperature, and has low energy consumption and a long device operation cycle.

Description

Technical Field

[0001] The invention relates to a jet fuel composition and a preparation method thereof. Background Art

[0002] Heavy petroleum fractions can be processed through fluid catalytic cracking (FCC) to produce light fractions such as liquefied gas and gasoline, and some catalytic cracking light cycle oil (catalytic cracking diesel) will also be produced as a by-product. As the severity of the catalytic cracking reaction increases, the H content and cetane number of the catalytic cracking light cycle oil will decrease significantly.

[0003] In order to make better use of catalytic cracking diesel, the conventional method is to mix a small amount of catalytic diesel with straight-run diesel and coking diesel for hydrogenation to produce automotive diesel. Under conventional hydrogenation conditions, the aromatic saturation rate of catalytic diesel is not high and the cetane number is not improved much, thus limiting the amount of catalytic cracking diesel added. Another method is to return the catalytic cracking diesel to the catalytic cracking reactor after hydrogenation for cracking reaction to increase the yield of catalytic gasoline.

[0004] In addition, hydrogenating catalytic cracking diesel to produce jet fuel is an effective and feasible means. Since the aromatic content of catalytic cracking diesel is high, the jet fuel prepared after hydrogenation has a higher density. CN105419865A discloses a method for producing jet fuel, which firstly hydrorefines the raw material and then performs hydrocracking, and fractionates the hydrocracking product to obtain jet fuel and diesel components.

[0005] CN10544127A discloses a method for producing jet fuel, which adopts one-stage hydrogenation refining and has a simple process flow.

[0006] In the prior art, in order to achieve high aromatic saturation, a higher reaction pressure is required, and as the operating time increases, the catalyst deactivates, and the reaction temperature needs to be continuously increased to maintain a certain aromatic saturation rate. Aromatic saturation is thermodynamically controlled, and high temperature is not conducive to aromatic saturation. The methods of the prior art have the problem of short operating cycles. Summary of the invention

[0007] The object of the present invention is to provide a jet fuel composition and a preparation method thereof based on the prior art.

[0008] In one aspect, the present invention provides a jet fuel composition, which comprises 5-20% by mass of C 9-18 Paraffins, 75-95% by mass C 9-18 Cycloalkanes and less than 7% by mass of C 9-18 Aromatic hydrocarbons; among which,

[0009] The content of the bicyclic cycloalkane is greater than or equal to 40% by mass based on the entire composition;

[0010] Based on the aromatic hydrocarbons in the composition, the content of the monocyclic aromatic hydrocarbons is greater than or equal to 90 mass %.

[0011] In a preferred case, based on the entire composition, C 9-18 The content of paraffin is 8-15% by mass, C 9-18 The content of cycloalkanes is 80-92% by mass.

[0012] In a preferred case, based on the entire composition, C 9-18 The aromatics content is less than or equal to 5 mass %.

[0013] In the present invention, the density of the composition measured at 20°C by standard method SH / T 0604-2000 is greater than 835 kg / m 3 .

[0014] In the present invention, the smoke point of the composition measured at 20°C by the standard method GB / T382-2017 is greater than 20 mm, and the net calorific value of the composition is greater than 42.9 MJ / kg.

[0015] In one embodiment of the present invention, the sulfur content of the composition is less than 1 mg / kg, and the nitrogen content is less than 1 mg / kg.

[0016] The jet fuel composition provided by the invention can meet the requirements of GJB1603 No. 6 jet fuel standard, has low contents of sulfur, nitrogen and aromatic hydrocarbons, and is a clean jet fuel composition.

[0017] Another aspect of the present invention provides a method for preparing any of the above jet fuel compositions, comprising the following steps:

[0018] (1) Catalytic cracking light cycle oil, hydroprocessing cycle oil and hydrogen are mixed and then introduced into a hydroprocessing reactor, and hydrodesulfurization, hydrodenitrogenation and partial aromatic saturation reactions are carried out under the action of a hydroprocessing catalyst, wherein the distillation range of the catalytic cracking light cycle oil is between 170° C. and 300° C., wherein the hydroprocessing catalyst comprises a carrier and a hydrogenation active component supported on the carrier, wherein the hydrogenation active component is selected from at least one metal of Group VIB and at least one metal of Group VIII, and wherein the carrier is selected from one or more of alumina, silicon oxide and titanium oxide;

[0019] (2) The reaction effluent of the hydroprocessing reactor is separated to remove impurity gases dissolved in the hydroprocessed oil to obtain a hydroprocessed oil having a sulfur content of less than 10 mg / kg. Part of the hydroprocessed oil is returned to step (1) as hydroprocessing circulating oil, and the remaining hydroprocessed oil enters a hydrodearomatization reactor.

[0020] (3) The hydrotreated oil obtained in step (2) enters a hydrodearomatization reactor, and undergoes a hydrodearomatization reaction under the action of a hydrodearomatization catalyst. The reaction effluent of the hydrodearomatization reactor is subjected to gas-liquid separation, and the obtained liquid phase material is fractionated to obtain a jet fuel composition.

[0021] In one embodiment of the present invention, the distillation range of the catalytic cracking light cycle oil is between 190-280°C.

[0022] In one embodiment of the present invention, the paraffin content in the catalytic cracking light cycle oil is less than 20% by mass, the aromatic content is greater than 70% by mass, and the mass fraction of bicyclic aromatics is greater than 50% based on the mass of total aromatics.

[0023] In one embodiment of the present invention, the aromatic content in the catalytic cracking light cycle oil is 80-90% by mass, and the paraffin content is 5-15% by mass.

[0024] In one embodiment of the present invention, the hydrogenation active components in the hydroprocessing catalyst are nickel, molybdenum and tungsten; based on the weight of the hydroprocessing catalyst, the content of molybdenum and tungsten is 20-40% by weight, and the content of nickel is 1-10% by weight, calculated as oxides.

[0025] In one embodiment of the present invention, the hydroprocessing reaction conditions are: reaction temperature 250-380°C, hydrogen partial pressure 3.2-6.4 MPa, liquid hourly volume space velocity 0.1-2.0 h -1 , the volume ratio of hydrogen to oil is 800-2000, and the mass ratio of hydrotreated cycle oil to catalytic cracking light cycle oil is 1-5:1.

[0026] According to the method provided by the present invention, the hydroprocessing reactor is a fixed bed reactor comprising at least two catalyst beds, and cold hydrogen can be injected between the beds.

[0027] The hydrogenation saturation of aromatics is a highly exothermic chemical reaction, and high temperature is not conducive to the saturation reaction of aromatics. When there is a liquid phase, the speed at which hydrogen diffuses to the catalyst surface through the liquid film is a controlling factor that affects the hydrogenation saturation of aromatics. The hydrogen consumption of aromatics hydrogenation is very high. In order to improve the efficiency of aromatics hydrogenation in the prior art, a higher hydrogen partial pressure is usually used to achieve it. Although a high hydrogen partial pressure is conducive to the diffusion of hydrogen into the liquid, a high operating pressure is also likely to cause the thickening of the liquid film, which increases the difficulty of hydrogen diffusion to the catalyst surface, resulting in a decrease in the hydrogenation saturation rate. In the present invention, it is preferred to use a hydroprocessing oil circulation method to increase the solubility of hydrogen in the liquid phase, thereby improving the solubility of hydrogen in the liquid phase under low pressure. In addition, the use of a hydroprocessing oil circulation method can also reduce the temperature rise of the catalyst bed, so that the reaction is carried out at a lower average reaction temperature, thereby improving the saturation rate of aromatics.

[0028] The present invention can realize the hydrodesulfurization, hydrodenitrogenation and partial aromatic saturation of crude oil at a medium pressure level by adopting the preferred hydrotreating catalyst and circulation ratio. By controlling the hydrotreating reaction conditions, the sulfur content of the raw material can be reduced to below 10 mg / kg and the aromatic content can be reduced to below 30%.

[0029] In a preferred case, the aromatic content of the hydrotreated oil is less than 25% by mass.

[0030] In one embodiment of the present invention, the reaction effluent after hydrogenation treatment is separated into gas and liquid by a high-pressure separator, and the separated gas is desulfurized and used as circulating hydrogen. The separated liquid phase logistics is further used to remove a certain amount of impurity gases such as hydrogen sulfide and ammonia dissolved in the liquid phase logistics, and a stripping tower or an adsorbent is selected for the removal process.

[0031] In the present invention, the hydrotreated oil obtained in step (2) enters a hydrodearomatization reactor and undergoes a hydroaromatic saturation reaction under the action of a hydroaromatic saturation catalyst. The smoke point of jet fuel is closely related to the content of aromatics. In the present invention, the aromatics in the hydrotreated oil are deeply saturated to obtain a jet fuel composition with a qualified smoke point.

[0032] In one embodiment of the present invention, the aromatic hydrogenation saturation catalyst uses alumina-silicon oxide as a carrier, and the active metal components are platinum and palladium. The content of platinum and palladium is 0.1-0.5% by weight, calculated as oxides and based on the aromatic hydrogenation saturation catalyst.

[0033] In one embodiment of the present invention, the hydrodearomatization reaction conditions are: reaction temperature 150-250°C, hydrogen partial pressure 3.2-6.4 MPa, volume space velocity 0.1-5.0 h -1 , the volume ratio of hydrogen to oil is 800-2000.

[0034] According to the method provided by the present invention, the hydrodearomatization reactor is a fixed bed reactor comprising at least two catalyst beds, and cold hydrogen can be injected between the beds.

[0035] In one embodiment of the present invention, the liquid phase material obtained after separation of the reaction effluent of the hydrodearomatization reactor is used as circulating oil, and the mass ratio of circulating oil to hydrotreated oil is 0-2: 1. It is preferred to use circulating oil to increase the solubility of hydrogen and reduce the temperature rise of the catalyst bed.

[0036] Features of the present invention:

[0037] The jet fuel composition provided by the invention can meet the requirements of GJB1603 No. 6 jet fuel standard, has low contents of sulfur, nitrogen and aromatic hydrocarbons, and is a clean jet fuel composition.

[0038] In the preparation method provided by the present invention, the catalytic cracking light cycle oil is subjected to hydrogenation treatment and then hydrogenation dearomatization, and the reaction product is subjected to gas-liquid separation and fractionation to obtain a jet fuel composition. The present invention can obtain high-density jet fuel components at a lower operating pressure and a lower reaction temperature, and has low energy consumption and a long device operation cycle. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 It is a schematic diagram of one embodiment of the method for preparing a jet fuel composition provided by the present invention. DETAILED DESCRIPTION

[0040] The present invention will be further described below in conjunction with the accompanying drawings, but the present invention is not limited thereby.

[0041] Figure 1 FIG. 1 is a schematic diagram of one embodiment of the method for preparing a jet fuel composition provided by the present invention, such as Figure 1 As shown, catalytic cracking light cycle oil 1 and hydroprocessing cycle oil 2 are mixed with circulating hydrogen 3 and heated to a certain temperature before entering into a hydroprocessing reactor 4. The hydroprocessing reactor is filled with a hydroprocessing catalyst, and hydrodesulfurization, hydrodenitrogenation and aromatic saturation reactions are carried out under appropriate reaction conditions. Cold hydrogen 5 can be injected between the catalyst beds. The reaction effluent 6 of the hydroprocessing reactor is separated into liquid products 8 and gas products 9 after passing through a gas-liquid separator 7; the gas product 9 is mixed with new hydrogen 10 after removing hydrogen sulfide and ammonia, and then pressurized by a circulating compressor 11 and used as circulating hydrogen 3. The liquid product 8 enters a stripper 12 to remove dissolved hydrogen sulfide, ammonia and other gases 13 to obtain hydroprocessed oil, a part of which is used as circulating oil 2, and the remaining hydroprocessed oil 14 enters a hydrodearomatization reactor 17.

[0042] The hydrotreated oil 14 and the circulating oil 15 are mixed with the circulating hydrogen 16 and then heated before entering the hydrodearomatization reactor 17. The hydrodearomatization reactor is filled with a hydrogenation aromatic saturation catalyst, and deep aromatic saturation is carried out under appropriate reaction conditions. Cold hydrogen 18 can be injected between the catalyst beds. The reaction effluent 19 of the hydrodearomatization reactor is separated into a liquid product and a gas product 22 through a gas-liquid separator 20. The gas product 22 and the new hydrogen 23 are mixed and then passed through a circulating compressor 24 for use as circulating hydrogen 16. The liquid product obtained by the gas-liquid separator 20 can be partially used as the circulating oil 15, and the remaining liquid product 21 enters a fractionation tower 25, and is fractionated to obtain a light fraction 26 and a jet fuel composition 27.

[0043] The following examples will further illustrate the method provided by the present invention, but are not intended to limit the present invention.

[0044] Unless otherwise specified, all reagents used in the examples are pure chemical reagents.

[0045] The hydrogenation active components were determined by X-ray fluorescence spectroscopy.

[0046] The hydroprocessing catalyst used was RSA-100 catalyst, produced by the Changling Catalyst Branch of Sinopec Catalyst Company. Based on the weight of the hydroprocessing catalyst, calculated as oxide, WO 3 Content 26%, MoO 3 The content is 2.5% and the NiO content is 2.6%.

[0047] The preparation method of the hydrogenation aromatics saturation catalyst is as follows:

[0048] The porous silicon oxide-alumina was prepared according to Example 1 of CN1510112A and the catalyst was prepared according to Example 7. In the prepared catalyst, SiO 2 Content 32.5 wt%, M SiO2 =0.45, B = 4.7Acmg -1 , k = 10.4, specific surface area 189m 2 / g, pore volume 0.46mL / g, average pore diameter 97A, Pt content 0.5 wt%, Pd content 0.3%, Pd / (pd+Pt) mass ratio 0.38. The catalyst was in-situ reduced at 450°C for 4 hours before use.

[0049] Example 1

[0050] Using feedstock 1 (catalytic cracking light cycle oil), 100 mL of hydroprocessing catalyst RSA-100 was installed in the hydroprocessing reactor. After the catalyst was sulfided, the reaction temperature was 340 °C, the liquid hourly volume space velocity was 0.5 h -1 The hydroprocessing reaction is carried out under the conditions of a volume ratio of 1000 to hydrogen oil and a circulation ratio (mass ratio of hydroprocessing circulating oil to raw material 1) of 2:1. The reaction effluent of the hydroprocessing reactor is separated, and the impurity gas dissolved in the hydroprocessing oil is removed to obtain a hydroprocessing oil with a sulfur content of less than 10 mg / kg. Part of the hydroprocessing oil is returned to the hydroprocessing reactor as hydroprocessing circulating oil, and the remaining hydroprocessing oil enters the hydrodearomatization reactor. The raw material properties are shown in Table 1, and the specific reaction conditions and hydroprocessing oil properties are shown in Table 2.

[0051] The hydrodearomatization reactor was filled with 100 mL of the prepared hydrogenation aromatic saturation catalyst. After the catalyst was reduced with hydrogen, the hydrotreated oil was heated to 5.0 MPa under a hydrogen partial pressure of 200 °C and a liquid hourly space velocity of 0.5 h -1The aromatic saturation reaction was carried out under the conditions of a hydrogen-oil volume ratio of 1000 and a circulation ratio (mass ratio of circulating oil to hydrotreated oil) of 2:1. The reaction effluent of the hydrodearomatization reactor was subjected to gas-liquid separation, and the obtained liquid phase material was used as circulating oil, and the remaining part was fractionated to obtain a jet fuel composition. The specific reaction conditions and product properties are shown in Table 3.

[0052] It can be seen from Table 3 that the jet fuel composition obtained in this example can meet the requirements of the GJB1603 No. 6 jet fuel standard.

[0053] Example 2

[0054] Using feedstock 1 (catalytic cracking light cycle oil), 100 mL of hydroprocessing catalyst RSA-100 was installed in the hydroprocessing reactor. After the catalyst was sulfided, the reaction temperature was 350 °C, the liquid hourly volume space velocity was 1.0 h -1 The hydroprocessing reaction is carried out under the conditions of a volume ratio of 1200 to hydrogen oil and a circulation ratio (mass ratio of hydroprocessing circulating oil to raw material 1) of 1:1. The reaction effluent of the hydroprocessing reactor is separated, and the impurity gas dissolved in the hydroprocessing oil is removed to obtain a hydroprocessing oil with a sulfur content of less than 10 mg / kg. Part of the hydroprocessing oil is returned to the hydroprocessing reactor as hydroprocessing circulating oil, and the remaining hydroprocessing oil enters the hydrodearomatization reactor. The raw material properties are shown in Table 1, and the specific reaction conditions and hydroprocessing oil properties are shown in Table 2.

[0055] The hydrodearomatization reactor was filled with 100 mL of the prepared hydrogenation aromatic saturation catalyst. After the catalyst was reduced with hydrogen, the hydrotreated oil was heated to 6.4 MPa under a hydrogen partial pressure, a reaction temperature of 200 °C, and a liquid hourly volume space velocity of 1.0 h -1 The aromatic saturation reaction was carried out under the conditions of a hydrogen-oil volume ratio of 1200 and a circulation ratio (mass ratio of circulating oil to hydrotreated oil) of 1:1. The reaction effluent of the hydrodearomatization reactor was subjected to gas-liquid separation, and the obtained liquid phase material was used as circulating oil, and the remaining part was fractionated to obtain a jet fuel composition. The specific reaction conditions and product properties are shown in Table 3.

[0056] It can be seen from Table 3 that the jet fuel composition obtained in this example can meet the requirements of the GJB1603 No. 6 jet fuel standard.

[0057] Comparative Example 1

[0058] Using feedstock 1 (catalytic cracking light cycle oil), 100 mL of hydroprocessing catalyst RSA-100 was installed in the hydroprocessing reactor. After the catalyst was sulfided, the reaction temperature was 350 °C, the liquid hourly volume space velocity was 1.0 h -1The hydroprocessing reaction was carried out under the condition of a hydrogen-to-oil volume ratio of 1200, and the reaction effluent of the hydroprocessing reactor was separated to remove the impurity gas dissolved in the hydroprocessing oil to obtain a hydroprocessing oil with a sulfur content of less than 10 mg / kg, and all the hydroprocessing oil entered the hydrodearomatization reactor. The specific reaction conditions and properties of the hydroprocessing oil are shown in Table 2.

[0059] The hydrodearomatization reactor was filled with 100 mL of the prepared hydrogenation aromatic saturation catalyst. After the catalyst was reduced with hydrogen, the hydrotreated oil was heated to 6.4 MPa under a hydrogen partial pressure, a reaction temperature of 200 °C, and a liquid hourly volume space velocity of 1.0 h -1 Aromatic saturation reaction was carried out under the condition of hydrogen to oil volume ratio of 1200. The reaction effluent of the hydrodearomatization reactor was subjected to gas-liquid separation, and the obtained liquid phase material was fractionated to obtain the product. The specific reaction conditions and product properties are shown in Table 3.

[0060] It can be seen from Table 3 that the product obtained in this comparative example cannot meet the requirements of the GJB1603 No. 6 jet fuel standard.

[0061] Comparative Example 2

[0062] Using feedstock 2 (catalytic cracking light cycle oil), 100 mL of hydroprocessing catalyst RSA-100 was installed in the hydroprocessing reactor. After the catalyst was sulfided, the reaction temperature was 340 °C, the liquid hourly volume space velocity was 1.0 h -1 The hydroprocessing reaction is carried out under the conditions of a volume ratio of 1000 to hydrogen oil and a circulation ratio (mass ratio of hydroprocessing circulating oil to raw material 2) of 2:1. The reaction effluent of the hydroprocessing reactor is separated, and the impurity gas dissolved in the hydroprocessing oil is removed to obtain a hydroprocessing oil with a sulfur content of less than 10 mg / kg. Part of the hydroprocessing oil is returned to the hydroprocessing reactor as hydroprocessing circulating oil, and the remaining hydroprocessing oil enters the hydrodearomatization reactor. The raw material properties are shown in Table 1, and the specific reaction conditions and hydroprocessing oil properties are shown in Table 2.

[0063] The hydrodearomatization reactor was filled with 100 mL of the prepared hydrogenation aromatic saturation catalyst. After the catalyst was reduced with hydrogen, the hydrotreated oil was heated to 6.4 MPa under a hydrogen partial pressure, a reaction temperature of 200 °C, and a liquid hourly volume space velocity of 1.0 h -1 Aromatic saturation reaction was carried out under the conditions of hydrogen-oil volume ratio of 1000 and circulation ratio (mass ratio of circulating oil to hydrotreated oil) of 1:1. The reaction effluent of the hydrodearomatization reactor was subjected to gas-liquid separation, and the obtained liquid phase material was used as circulating oil, and the remaining part was fractionated to obtain the product. The specific reaction conditions and product properties are shown in Table 3.

[0064] It can be seen from Table 3 that the product obtained in this comparative example cannot meet the requirements of the GJB1603 No. 6 jet fuel standard.

[0065] Table 1

[0066] project Raw material 1 Raw material 2 <![CDATA[Density (20 °C), kg / m 3 > 924.0 911.0 Sulfur content, mg / kg 3060 6500 Nitrogen content, mg / kg 203 195 Distillation range, ℃ Initial distillation point 192 187 10％ 224 213 50％ 243 231 90％ 258 255 Final distillation point 272 273 Hydrocarbon composition, mass % Alkanes 12.7 11.0 Cycloalkanes 5.0 5.3 Monocyclic aromatic hydrocarbons 37.4 54.3 Bicyclic aromatic hydrocarbons 44.7 29.1 Total aromatics 82.3 83.7

[0067] Table 2

[0068]

[0069]

[0070] Table 3

[0071]

[0072]

Claims

1. A method for preparing a jet fuel composition, comprising the following steps: (1) Catalytic cracking light cycle oil, hydrotreated cycle oil and hydrogen are mixed and then introduced into a hydroprocessing reactor, and hydrodesulfurization, hydrodenitrogenation and partial aromatic saturation reactions are carried out under the action of a hydroprocessing catalyst, the distillation range of the catalytic cracking light cycle oil is between 170-300° C., the paraffin content in the catalytic cracking light cycle oil is less than 20% by mass, the aromatic content is greater than 70% by mass, the mass fraction of bicyclic aromatics is greater than 50% based on the mass of total aromatics, the mass ratio of the hydrotreated cycle oil to the catalytic cracking light cycle oil is 1-5:1, the hydroprocessing catalyst comprises a carrier and a hydrogenation active component supported on the carrier, the hydrogenation active component is selected from at least one metal of Group VIB and at least one metal of Group VIII, and the carrier is selected from one or more of alumina, silicon oxide and titanium oxide; (2) The reaction effluent of the hydroprocessing reactor is separated to remove impurity gases dissolved in the hydroprocessed oil to obtain a hydroprocessed oil having a sulfur content of less than 10 mg / kg. Part of the hydroprocessed oil is returned to step (1) as hydroprocessing circulating oil, and the remaining hydroprocessed oil enters a hydrodearomatization reactor. (3) the hydrotreated oil obtained in step (2) enters a hydrodearomatization reactor, performs a hydrodearomatization reaction under the action of a hydrodearomatization catalyst, performs gas-liquid separation on the reaction effluent of the hydrodearomatization reactor, and fractionates the obtained liquid phase material to obtain a jet fuel composition; The jet fuel composition comprises 5-20 mass % of C 9-18 Paraffins, 75-95% by mass C 9-18 Cycloalkanes and less than 7 mass% of C 9-18 Aromatic hydrocarbons; among which, The content of the bicyclic cycloalkane is greater than or equal to 40% by mass based on the entire composition; Based on the aromatic hydrocarbons in the composition, the content of the monocyclic aromatic hydrocarbons is greater than or equal to 90 mass %.

2. The method according to claim 1, characterized in that Based on the overall composition, C 9-18 The content of paraffin is 8-15% by mass, C 9-18 The content of cycloalkanes is 80-92% by mass.

3. The method according to claim 1, characterized in that Based on the overall composition, C 9-18 Aromatic hydrocarbons are less than or equal to 5% by mass; The composition has a sulfur content of less than 1 mg / kg and a nitrogen content of less than 1 mg / kg.

4. The method according to claim 1, characterized in that: The density of the composition measured at 20°C by standard method SH / T 0604-2000 is greater than 835 kg / m 3 .

5. The method according to claim 1, characterized in that The smoke point of the composition measured at 20° C. by the standard method GB / T 382-2017 is greater than 20 mm, and the net calorific value of the composition is greater than 42.9 MJ / kg.

6. The method according to claim 1, characterized in that The distillation range of catalytic cracking light cycle oil is between 190-280℃.

7. The method according to claim 1, characterized in that The aromatic content in the catalytic cracking light cycle oil is 80-90% by mass, and the paraffin content is 5-15%.

8. The method according to claim 1, characterized in that The hydrogenation active components in the hydroprocessing catalyst are nickel, molybdenum and tungsten; based on the weight of the hydroprocessing catalyst, the content of molybdenum and tungsten is 20-40% by weight, and the content of nickel is 1-10% by weight, calculated as oxides.

9. The method according to claim 1, characterized in that: The reaction conditions of the hydroprocessing are: reaction temperature 250-380°C, hydrogen partial pressure 3.2-6.4MPa, liquid hourly volume space velocity 0.1-2.0h -1 , hydrogen to oil volume ratio 800-2000.

10. The method according to claim 1, characterized in that The aromatic content of the hydrotreated oil is less than 25% by mass.

11. The method according to claim 1, characterized in that: The hydrogenation aromatic saturation catalyst uses aluminum oxide-silicon oxide as a carrier, and the active metal components are platinum and palladium. The content of platinum and palladium is 0.1-0.5% by weight, calculated as oxides and based on the hydrogenation aromatic saturation catalyst.

12. The method according to claim 1, characterized in that The conditions for the hydrodearomatization reaction are: reaction temperature 150-250°C, hydrogen partial pressure 3.2-6.4MPa, volume space velocity 0.1-5.0h -1 , the volume ratio of hydrogen to oil is 800-2000.

13. The method according to claim 1, characterized in that The liquid phase material obtained after separation of the reaction effluent of the hydrodearomatization reactor is used as circulating oil, and the mass ratio of the circulating oil to the hydrotreated oil is 0-2:1.

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