Integrated universal fuel and preparation method and system thereof

Abstract

Integrated general fuel and its preparation method and system. Its indexes are as follows: density at 20℃ is 0.775-0.830 g / cm 3 ; freezing point ≤-47℃; net heat value ≥42.8 MJ / Kg; cetane number ≥45; condensation point ≤-50℃; cold filter plugging point ≤-50℃; closed flash point ≥50℃; polycyclic aromatic hydrocarbon content ≤1 wt%; 10% recovery temperature ≤205℃; 50% recovery temperature ≤232℃; final boiling point ≤300℃. Its preparation method comprises: (1) coal direct liquefaction oil is subjected to fractionation, hydrofining and separation in sequence to obtain coal direct liquefaction full distillate; (2) coal indirect liquefaction oil is subjected to the foregoing process to obtain coal indirect liquefaction full distillate; (3) coal direct and indirect liquefaction full distillates are cut and blended. The integrated general fuel meets the main indexes of diesel and jet fuel; its preparation method and system are simple and low in cost.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of coal-based fuel, and particularly relates to an integrated universal fuel and a preparation method and a preparation system thereof. BACKGROUND

[0002] As military supplies, the current supply of oil requires to meet the requirements of rapidness, high efficiency, timeliness and accuracy. Due to the application of a large number of mechanization and advanced equipment, the quality and performance requirements of oil are higher and higher, and the oil supply task is very difficult. In the existing military fuel supply system, different fuels are generally used to supply oil to equipment, and too many fuel varieties have become a difficult problem that plagues oil supply, management and use, and brings great trouble to oil supply work. The use of integrated universal fuel can simplify logistics supply support, improve the combat readiness of equipment, and be conducive to the coordinated operation and joint operation of different military services. At present, the US army has developed and used a single variety of aviation fuel suitable for tanks, ground vehicles, aircraft and some ships. China has also carried out related research on integrated universal fuel, but it has not been popularized and used in the army.

[0003] Diesel engines mainly use diesel, and aviation turbine engines use jet fuel, both of which have similar distillates and components. The idea of using integrated universal fuel on diesel engines and aviation turbine engines is based on the use of one kind of integrated universal fuel in most equipment to facilitate logistics support, simplify oil delivery procedures, shorten supply time and other military effects. The replacement plan is not to completely eliminate other fuels, but to change the main military diesel engine equipment and aviation equipment to use the same fuel.

[0004] From the demand of military oil, with the rapid development of military aircraft and ground equipment in China, higher requirements for the power and other properties of fuel are put forward, and a series of characteristics such as high density, high energy, better propulsion and better volume properties are required. The traditional military fuel is generally obtained by processing and cutting crude oil to a certain extent, but due to the structure of its own composition, the density, energy and other properties have reached the limit, and the high temperature thermal stability and low temperature of petroleum base material also have inherent defects, which to some extent affect its performance.

[0005] There are many processes for preparing coal-based diesel or coal-based jet fuel in the prior art, but there is no technology for preparing integrated universal fuel meeting the main indicators of diesel and jet fuel by using coal liquefied oil as raw material. SUMMARY

[0006] The first object of the present application is to provide an integrated general fuel which can meet the main indexes of diesel and jet fuel at the same time, can be used for the logistic supply and oil supply guarantee of the equipment needing diesel and jet fuel, can simplify the oil delivery procedure, and can shorten the supply time and other military effects.

[0007] The second object of the present application is to provide a preparation method of the aforementioned integrated general fuel, which is simple in process and is beneficial to reduce the equipment and cost.

[0008] The third object of the present application is to provide a preparation system of the aforementioned integrated general fuel, which is simple and easy to operate, has less equipment, and is low in cost.

[0009] To achieve the first object of the present application, the following technical scheme is adopted:

[0010] An integrated general fuel, whose parameters are as follows:

[0011] The density at 20℃ is 0.775-0.830 g / cm 3 ;

[0012] The freezing point is ≤-47℃;

[0013] The net heat value is ≥42.8 MJ / Kg;

[0014] The cetane number is ≥45;

[0015] The freezing point is ≤-50℃;

[0016] The cold filter point is ≤-50℃;

[0017] The closed flash point is ≥50℃;

[0018] The polycyclic aromatic hydrocarbon content is ≤1 wt%;

[0019] The 10% recovery temperature is ≤205℃;

[0020] The 50% recovery temperature is ≤232℃;

[0021] The final boiling point is ≤300℃.

[0022] To achieve the second object of the present application, the following technical scheme is adopted:

[0023] A preparation method of the aforementioned integrated general fuel, comprising the following steps:

[0024] (1) Directly liquefying coal oil, then performing fractionation on the obtained light distillate oil, then performing hydrofining on the obtained light distillate oil, and then separating the obtained refined product stream to obtain coal direct liquefaction full distillate oil;

[0025] (2) fractionating the coal indirect liquefaction oil, then hydrorefining the obtained light fraction oil, and separating the obtained refined product stream to obtain a coal indirect liquefaction full distillate oil;

[0026] (3) fractionating and mixing the coal direct liquefaction full distillate oil obtained in step (1) and the coal indirect liquefaction full distillate oil obtained in step (2) in any order to obtain an integrated general-purpose fuel.

[0027] In the preparation method of the present application, preferably, in step (1), the heavy fraction oil obtained by fractionating the coal direct liquefaction oil is sent to a solvent hydrostabilization reactor as a solvent to perform solvent hydrostabilization to output a circulating solvent.

[0028] In the preparation method of the present application, preferably, in step (1), the fractionation temperature of the coal direct liquefaction oil is 300-350℃.

[0029] In the preparation method of the present application, preferably, in step (1), the reaction temperature of the hydrorefining is 320-400℃, and / or the reaction pressure is 6.0-20.0 MPa, and / or the volume space velocity is 0.5-4.0 h -1 , and / or the hydrogen / oil ratio is 500-1500 V / V.

[0030] In the preparation method of the present application, preferably, in step (2), the fractionation temperature of the coal indirect liquefaction oil is 320-350℃.

[0031] In the preparation method of the present application, preferably, in step (2), the reaction temperature of the hydrorefining is 300-350℃, and / or the reaction pressure is 5.0-10.0 MPa, and / or the volume space velocity is 0.5-4.0 h -1 , and / or the hydrogen / oil ratio is 200-800 V / V.

[0032] In the preparation method of the present application, preferably, in step (1), the hydrorefining is continuously performed twice.

[0033] In the preparation method of the present application, preferably, in step (1), the coal direct liquefaction oil is a coal direct liquefaction oil prepared by direct liquefaction reaction of coal.

[0034] In the preparation method of the present application, preferably, in step (2), the hydrorefining is continuously performed twice.

[0035] In the preparation method of the present application, preferably, in step (2), the coal indirect liquefaction oil is a coal indirect liquefaction oil prepared by Fischer-Tropsch synthesis reaction of synthesis gas.

[0036] The preparation method of the present application, preferably, in step (3), the coal direct liquefaction full distillate oil obtained in step (1) and the coal indirect liquefaction full distillate oil obtained in step (2) are first fractionally cut respectively, light components are discharged, and the coal direct liquefaction product oil and the coal indirect liquefaction product oil are obtained; then the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil are mixed and blended to obtain the integrated general fuel.

[0037] The preparation method of the present application, further preferably, in step (3), when the coal direct liquefaction full distillate oil obtained in step (1) is fractionally cut, the lower limit of the fractionation temperature is 150-180℃, and the upper limit is 260-300℃; and / or,

[0038] In step (3), when the coal indirect liquefaction full distillate oil obtained in step (2) is fractionally cut, the lower limit of the fractionation temperature is 150-180℃, and the upper limit is 260-300℃; and / or,

[0039] In step (3), the blending ratio of the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil is 1:9-9:1 in terms of mass ratio.

[0040] The preparation method of the present application, preferably, in step (3), the coal direct liquefaction full distillate oil obtained in step (1) and the coal indirect liquefaction full distillate oil obtained in step (2) are first mixed and blended; then the obtained mixed oil is fractionally cut, light components are discharged, and the integrated general fuel is obtained.

[0041] The preparation method of the present application, further preferably, in step (3), the blending ratio of the coal direct liquefaction full distillate oil obtained in step (1) and the coal indirect liquefaction full distillate oil obtained in step (2) is 1:9-9:1 in terms of mass ratio; and / or,

[0042] In step (3), when the obtained mixed oil is fractionally cut, the lower limit of the fractionation temperature is 150-180℃, and the upper limit is 260-300℃.

[0043] To achieve the third object of the present application, a preparation system for the aforementioned preparation method is also provided.

[0044] The present application has the following beneficial effects:

[0045] The integrated general fuel of the present application can simultaneously meet the main indicators of diesel and jet fuel, and can be used for logistics supply and oil supply guarantee of equipment requiring diesel and jet fuel, thereby simplifying the oil delivery procedure, shortening the supply time and other military effects;

[0046] The preparation method and preparation system of the integrated general fuel can prepare the integrated general fuel by combining mixing and blending with fractionation cutting, and the process is simple, only a hydrogenation refining reactor is needed in the preparation process, without a coal direct liquefaction hydrogenation modification reactor and a coal indirect liquefaction hydrogenation cracking and condensation reduction reactor, so that the equipment investment is reduced, the preparation process is shortened, and the preparation cost is reduced. BRIEF DESCRIPTION OF DRAWINGS

[0047] Figure 1 is a flow diagram of the preparation method of the integrated general fuel in one embodiment of the present application; and is a structural diagram of the preparation system of the integrated general fuel in one embodiment of the present application;

[0048] Figure 2 is a flow diagram of the preparation method of the integrated general fuel in another embodiment of the present application; and is a structural diagram of the preparation system of the integrated general fuel in another embodiment of the present application. DETAILED DESCRIPTION

[0049] The technical solutions of the present application and the effects thereof will be further described below in combination with specific embodiments / examples and the drawings. The following embodiments / examples are only used to illustrate the content of the present application, and the present application is not limited to the following embodiments or examples. Simple changes of the present application by applying the concept of the present application are within the scope of the present application.

[0050] The present application provides an integrated general fuel, and the parameters are as follows:

[0051] The density at 20℃ is 0.775-0.830 g / cm 3 ;

[0052] The freezing point is ≤-47℃;

[0053] The net heat value is ≥42.8 MJ / Kg;

[0054] The cetane number is ≥45;

[0055] The freezing point is ≤-50℃;

[0056] The cold filter point is ≤-50℃;

[0057] The closed flash point is ≥50℃;

[0058] The polycyclic aromatic hydrocarbon content is ≤1 wt%;

[0059] The 10% recovery temperature is ≤205℃;

[0060] The 50% recovery temperature is ≤232℃;

[0061] The final boiling point is ≤300℃.

[0062] The integrated general fuel of the present application can meet the main indexes of diesel and jet fuel at the same time, and can be used for the logistics supply and oil supply guarantee of the equipment needing diesel and jet fuel, simplifying the oil delivery procedure, shortening the supply time and other military effects.

[0063] The present application also provides a preparation method of the aforementioned integrated general fuel, as shown in Figure 1 、 2 The preparation method comprises the following steps:

[0064] (1) subjecting the direct coal liquefaction oil to fractionation, then subjecting the obtained light fraction oil to hydrofining, and then subjecting the obtained hydrofining product stream to separation to obtain a direct coal liquefaction full fraction oil;

[0065] (2) subjecting the indirect coal liquefaction oil to fractionation, then subjecting the obtained light fraction oil to hydrofining, and then subjecting the obtained hydrofining product stream to separation to obtain an indirect coal liquefaction full fraction oil;

[0066] (3) subjecting the direct coal liquefaction full fraction oil obtained in step (1) and the indirect coal liquefaction full fraction oil obtained in step (2) to fractionation cutting and mixing in any order to obtain the integrated general fuel.

[0067] The preparation method of the integrated general fuel of the present application can prepare the aforementioned integrated general fuel, and the process is simple, only a hydrofining reactor needs to be provided in the preparation process, and no direct coal liquefaction hydro-upgrading reactor and indirect coal liquefaction hydrocracking and pour point depressing reactor are needed, thereby reducing the equipment investment, shortening the preparation process and reducing the preparation cost.

[0068] In the present application, the "subjecting the direct coal liquefaction full fraction oil obtained in step (1) and the indirect coal liquefaction full fraction oil obtained in step (2) to fractionation cutting and mixing in any order" in step (3) means that the direct coal liquefaction full fraction oil obtained in step (1) and the indirect coal liquefaction full fraction oil obtained in step (2) can be processed in the following two orders: order one, subjecting the direct coal liquefaction full fraction oil obtained in step (1) and the indirect coal liquefaction full fraction oil obtained in step (2) to fractionation cutting first, and then subjecting the cut fractions to mixing; order two, subjecting the direct coal liquefaction full fraction oil obtained in step (1) and the indirect coal liquefaction full fraction oil obtained in step (2) to mixing first, and then subjecting the mixed oil to fractionation cutting.

[0069] Those skilled in the art will appreciate that due to differences in production processes, the properties of direct coal liquefaction oil and indirect coal liquefaction oil differ significantly. Direct coal liquefaction oil is primarily composed of cycloalkyl groups, with advantages: high specific gravity, high volume calorific value, high thermal stability, and a low freezing point; disadvantages: low cetane index and slightly low net calorific value. Indirect coal liquefaction oil is primarily composed of straight-chain alkanes, with advantages: high cetane index; disadvantages: low specific gravity, high net calorific value, and a high freezing point. Neither of these two coal-based oils meets all the indicators of an integrated universal fuel. However, both coal-based oils are scarce resources, have special characteristics, and have excellent mutual solubility and complementary product performance. For example, the coal direct liquefaction diesel in coal direct liquefaction oil is a diesel fraction obtained by direct liquefaction of coal and solvent. In one embodiment, it is taken from the National Energy Group's million-ton coal direct liquefaction industrial demonstration unit process (Ordos); the coal indirect liquefaction diesel in coal indirect liquefaction oil is a diesel fraction obtained by Fischer-Tropsch synthesis of hydrogen and carbon monoxide (synthesis gas). In one embodiment, it is taken from the National Energy Group Ningxia Coal Industry Coal Indirect Liquefaction Unit.

[0070] In the existing process for processing direct coal liquefaction oil, after passing through the hydrofining reactor, it needs to enter a hydro-upgrading reactor. Hydrofining is mainly for removing non-hydrocarbon compounds such as sulfur, nitrogen, and oxygen in the oil product, as well as saturating aromatic hydrocarbons, while hydro-upgrading is for increasing the cetane number and reducing the density and pour point. In the preparation method of the present invention, although the direct coal liquefaction oil has a high density and a low cetane number, it can neutralize the related defects of the existing process after fractionation and blending with the indirect coal liquefaction oil. Therefore, in step (1) of the present invention, after hydrofining, there is no need to perform hydro-upgrading again, so only a hydro-finishing reactor needs to be set up, and there is no need to set up a hydro-upgrading reactor after the hydro-finishing reactor, which is beneficial to reducing costs.

[0071] In the existing process for the treatment of indirect coal liquefaction oil, after passing through the hydrorefining reactor, it is necessary to enter a hydrocracking reactor and a pour point depressing reactor. The hydrorefining is mainly to remove oxygen and heteroatoms from the Fischer-Tropsch synthesis oil, as well as the saturation of unsaturated hydrocarbons, while the function of hydrocracking and pour point depressing is to reduce the pour point. In the preparation method of the present invention, although the pour point of indirect coal liquefaction oil is high and the density of direct coal liquefaction oil is high and the cetane number is low, after fractionation and blending with direct coal liquefaction oil, the relevant defects in the existing process can be neutralized. Therefore, in step (3) of the present invention, after hydrorefining, there is no need to perform hydrocracking and pour point depressing. Therefore, only a hydrorefining reactor needs to be set, and there is no need to set a hydrocracking reactor and pour point depressing reactor after the hydrorefining reactor, which is conducive to reducing costs.

[0072] The person skilled in the art understands that the coal direct liquefaction oil has high density, good low-temperature fluidity, low net calorific value and low cetane number, while the coal indirect liquefaction oil has low density, poor low-temperature fluidity, high net calorific value and high cetane number, so the two kinds of fuels cannot meet the index requirements of the integrated general fuel. The present application can meet the index requirements of density, net calorific value and cetane number by blending the two kinds of fuels, and the freezing point and distillation range can be met by cutting and selecting the appropriate distillation fraction, so the preparation method of the present application can process the coal direct liquefaction oil and the coal indirect liquefaction oil to obtain the integrated general fuel meeting the index requirements by blending and cutting the two kinds of fuels.

[0073] In an embodiment of the preparation method of the present application, in step (1), the heavy fraction oil obtained by fractionating the coal direct liquefaction oil is sent to the hydrogenation stabilizing reactor as a solvent raw material to perform solvent hydrogenation stabilization to output a circulating solvent.

[0074] In an embodiment of the preparation method of the present application, in step (1), the fractionation temperature of the coal direct liquefaction oil is 300-350℃, such as 300℃, 310℃, 320℃, 330℃, 340℃ and 350℃ and any value and value range within the range.

[0075] In step (1) of the preparation method of the present application, the hydrogenation refining catalyst used for hydrogenation refining is a relatively common hydrogenation catalyst on the market, which functions to saturate aromatic hydrocarbons and remove heteroatoms such as sulfur and nitrogen in the crude oil. For example, in an embodiment, the hydrogenation refining catalyst used for hydrogenation refining in step (1) includes:

[0076] The catalyst carrier uses amorphous alumina or amorphous aluminum silicate;

[0077] The active metal loaded on the catalyst carrier is a non-noble metal of VIB and VIII groups; wherein the content of the VIB group non-noble metal component is 0.5-30wt%, such as 0.5wt%, 1wt%, 5wt%, 10wt%, 15wt%, 20wt%, 25wt% and 30wt% and any value and value range within the range; the content of the VIII group non-noble metal component is 1-20wt%, such as 1wt%, 5wt%, 10wt%, 15wt% and 20wt% and any value and value range within the range; and / or the VIB group non-noble metal is selected from Mo and / or W, and the VIII group non-noble metal is selected from Co and / or Ni.

[0078] For example, in an embodiment, the hydrogenation refining catalyst used for hydrogenation refining in step (1) is FFT-1B, which specifically includes:

[0079] The catalyst carrier uses amorphous alumina;

[0080] The Ni content is 6 wt%, and the Mo content is 20 wt%.

[0081] The preparation method of the present invention, in one embodiment, in step (1), the reaction temperature of the hydrofining is 320-400°C, such as 320°C, 330°C, 340°C, 350°C, 360°C, 370°C, 380°C, 390°C and 400°C and any numerical value and numerical range within the range; and / or the reaction pressure is 6.0-20.0 MPa, such as 6.0 MPa, 8.0 MPa, 10.0 MPa, 12.0 MPa, 14.0 MPa, 16.0 MPa, 18.0 MPa and 20.0 MPa and any numerical value and numerical range within the range; and / or the volume space velocity is 0.5-4.0 h -1 , for example 0.5h -1 , 1.0h -1 , 1.5h -1 , 2.0h -1 , 2.5h -1 , 3.0h -1 , 3.5h -1 , 4.0h -1 and any numerical value and numerical range within the range; and / or the hydrogen-to-oil ratio is 500-1500V / V, such as 500V / V, 600V / V, 700V / V, 800V / V, 900V / V, 1000V / V, 1100V / V, 1200V / V, 1300V / V, 1400V / V and 1500V / V and any numerical value and numerical range within the range.

[0082] In one embodiment of the preparation method of the present invention, in step (2), the distillation temperature of the coal indirect liquefaction oil is 320-350°C, such as 320°C, 330°C, 340°C and 350°C and any value and numerical range within this range.

[0083] In the preparation method of the present invention, the hydrorefining catalyst used in step (2) is a relatively common hydrogenation catalyst on the market, which functions to saturate aromatic hydrocarbons and remove heteroatoms such as sulfur and nitrogen in crude oil. For example, in one embodiment, in step (2), the hydrorefining catalyst used in the hydrorefining comprises:

[0084] The catalyst carrier is amorphous alumina or amorphous aluminum silicate;

[0085] The active metal supported on the catalyst carrier is a non-noble metal of VIB and VIII groups; wherein the content of the non-noble metal component of VIB group is 0.5-30wt%, such as 0.5wt%, 1wt%, 5wt%, 10wt%, 15wt%, 20wt%, 25wt% and 30wt% and any value and value range within the range; the content of the non-noble metal component of VIII group is 1-10wt%, such as 1wt%, 2wt%, 3wt%, 4wt%, 5wt%, 6wt%, 7wt%, 8wt%, 9wt% and 10wt% and any value and value range within the range; and / or the non-noble metal of VIB group is selected from Mo and / or W, and the non-noble metal of VIII group is selected from Co and / or Ni.

[0086] For example, in one embodiment, in step (2), the hydrofining catalyst used for hydrofining is FZC-3, which specifically comprises:

[0087] The catalyst carrier uses amorphous alumina;

[0088] The content of Ni is 4wt%, and the content of Mo is 15wt%.

[0089] In one embodiment of the preparation method of the present application, in step (2), the reaction temperature for hydrofining is 300-350℃, such as 300℃, 310℃, 320℃, 330℃, 340℃ and 350℃ and any value and value range within the range; and / or the reaction pressure is 5.0-10.0MPa, such as 5.0MPa, 6.0MPa, 7.0MPa, 8.0MPa, 9.0MPa and 10.0MPa and any value and value range within the range; and / or the volume space velocity is 0.5-4.0h -1 , such as 0.5h -1 , 1.0h -1 , 1.5h -1 , 2.0h -1 , 2.5h -1 , 3.0h -1 , 3.5h -1 , 4.0h -1 and any value and value range within the range; and / or the hydrogen / oil ratio is 200-800V / V, such as 200V / V, 300V / V, 400V / V, 500V / V, 600V / V, 700V / V and 800V / V and any value and value range within the range.

[0090] In one embodiment of the preparation method of the present application, in step (1), the hydrofining is continuously carried out for 2 times.

[0091] In an embodiment of the preparation method, in step (1), the coal direct liquefaction oil is a coal direct liquefaction oil prepared by a coal direct liquefaction reaction.

[0092] The coal direct liquefaction reaction is well known in the art, and can be specifically seen from the coal direct liquefaction method disclosed in CN 1598351A, which will not be described here.

[0093] In an embodiment of the preparation method, in step (2), the hydrofining is continuously performed twice.

[0094] In an embodiment of the preparation method, in step (2), the coal indirect liquefaction oil is a coal indirect liquefaction oil prepared by a Fischer-Tropsch synthesis reaction of the synthesis gas.

[0095] The Fischer-Tropsch synthesis reaction is well known in the art, and can be specifically seen from the coal indirect liquefaction crude oil prepared by the Fischer-Tropsch synthesis method and system disclosed in CN 101955788A.

[0096] In an embodiment of the preparation method, as shown in Figure 1 In step (3), the coal direct liquefaction whole distillate oil obtained in step (1) and the coal indirect liquefaction whole distillate oil obtained in step (2) are respectively subjected to fractional distillation cutting, light components are discharged, and coal direct liquefaction product oil and coal indirect liquefaction product oil are obtained; then the coal direct liquefaction product oil and the coal indirect liquefaction product oil are mixed and blended to obtain the integrated general fuel.

[0097] In a preferred embodiment, in step (3), when the coal direct liquefaction whole distillate oil obtained in step (1) is subjected to fractional distillation cutting, the lower limit of the fractional distillation temperature is 150-180°C, such as 150°C, 160°C, 170°C, 180°C, and any value and value range within the range; the upper limit is 260-300°C, such as 260°C, 270°C, 280°C, 290°C, and 300°C, and any value and value range within the range.

[0098] In a preferred embodiment, in step (3), when the coal indirect liquefaction whole distillate oil obtained in step (2) is subjected to fractional distillation cutting, the lower limit of the fractional distillation temperature is 150-180°C, such as 150°C, 160°C, 170°C, 180°C, and any value and value range within the range; the upper limit is 260-300°C, such as 260°C, 270°C, 280°C, 290°C, and 300°C, and any value and value range within the range.

[0099] In a preferred embodiment, in step (3), the blending ratio of the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil is 1:9-9:1 by mass, such as 1:9, 2:8, 3:7, 4:6, 5:5, 6:4, 7:3, 8:2, 9:1.

[0100] The preparation method of the present application, in an embodiment, as shown in Figure 2 Fig. 1, in step (3), the coal direct liquefaction full-range oil obtained in step (1) and the coal indirect liquefaction full-range oil obtained in step (2) are first mixed and blended; then the obtained mixed oil is subjected to fractional distillation cutting to discharge light components and obtain an integrated general fuel.

[0101] In a preferred embodiment, in step (3), the blending ratio of the coal direct liquefaction full-range oil obtained in step (1) and the coal indirect liquefaction full-range oil obtained in step (2) is 1:9-9:1 by mass, such as 1:9, 2:8, 3:7, 4:6, 5:5, 6:4, 7:3, 8:2, 9:1.

[0102] In a preferred embodiment, in step (3), when the obtained mixed oil is subjected to fractional distillation cutting, the lower limit of the fractional distillation temperature is 150-180℃, such as 150℃, 160℃, 170℃ and 180℃ and any value and value range within the range; the upper limit is 260-300℃, such as 260℃, 270℃, 280℃, 290℃ and 300℃ and any value and value range within the range.

[0103] The preparation method of the present application, the coal direct liquefaction and the coal indirect liquefaction have two different process routes. According to the existing industrial device situation, the coal direct liquefaction full-range oil and the coal indirect liquefaction full-range oil are mixed and blended after which fractional distillation cutting is performed to obtain an integrated general fuel with indicators meeting the standards, that is, the cutting process is performed after the blending process. If the overall industrialization is realized, the coal direct liquefaction full-range oil and the coal indirect liquefaction full-range oil can be directly subjected to fractional distillation cutting, and the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil are mixed and blended in a certain ratio to obtain an integrated general fuel with indicators meeting the standards, that is, the blending process is performed after the cutting process.

[0104] The present application also provides a preparation system for the aforementioned preparation method.

[0105] In an embodiment, as shown in Figure 1 Fig. 1, the preparation system comprises a first fractional distillation column 101, a first hydrofining reactor 102, a second hydrofining reactor 103, a first separation device 104, a second fractional distillation column 105 connected in sequence through pipelines;

[0106] The first fractionating column 101 is provided with a material inlet for feeding in coal direct liquefaction oil and fractionating the same, outputting light oil fraction and heavy oil fraction;

[0107] The first hydrofining reactor 102 is provided with a material inlet for feeding in hydrogen to perform first hydrofining on the light oil fraction from the first fractionating column 101, outputting first refined product thereof;

[0108] The second hydrofining reactor 103 is provided with a material inlet for feeding in the first refined product from the first hydrofining reactor 102 and performing second hydrofining thereon, outputting second refined product thereof as the refined product thereof;

[0109] The first separation device 104 is provided with a material inlet for feeding in the refined product from the second hydrofining reactor 103 and separating the same, discharging light components, outputting coal direct liquefaction full distillate oil;

[0110] The second fractionating column 105 is provided with a material inlet for feeding in coal direct liquefaction full distillate oil from the first separation device 104 and fractionating and cutting the same, discharging naphtha, outputting coal direct liquefaction product oil;

[0111] The preparation system further comprises a third fractionating column 201, a third hydrofining reactor 202, a fourth hydrofining reactor 203, a second separation device 204, a fourth fractionating column 205 connected in sequence through pipelines;

[0112] The third fractionating column 201 is provided with a material inlet for feeding in coal indirect liquefaction oil and fractionating the same, outputting light oil fraction and heavy oil fraction;

[0113] The third hydrofining reactor 202 is provided with a material inlet for feeding in hydrogen to perform first hydrofining on the light oil fraction from the third fractionating column 201, outputting first refined product thereof;

[0114] The fourth hydrofining reactor 203 is provided with a material inlet for feeding in the first refined product from the third hydrofining reactor 202 and performing second hydrofining thereon, outputting second refined product thereof as the refined product thereof;

[0115] The second separation device 204 is provided with a material inlet for feeding in the refined product from the fourth hydrofining reactor 203 and separating the same, discharging light components, outputting coal indirect liquefaction full distillate oil;

[0116] The fourth fractionating column 205 is provided with a material inlet for feeding in the coal indirect liquefaction full distillate oil from the second separation device 204 and fractionating and cutting the same, discharging naphtha, and outputting coal indirect liquefaction product oil;

[0117] The preparation system further comprises a mixer (not shown in the figure) for mixing and blending the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil, to obtain an integrated universal fuel.

[0118] In one embodiment, as shown in Figure 2 The preparation system comprises, connected in sequence through pipelines, a first fractionating column 101, a first hydrofining reactor 102, a second hydrofining reactor 103, and a first separation device 104.

[0119] The first fractionating column 101 is provided with a material inlet for feeding in coal direct liquefaction oil and fractionating the same, outputting light oil fraction and heavy oil fraction;

[0120] The first hydrofining reactor 102 is provided with a material inlet for feeding in hydrogen to perform first hydrofining on the light oil fraction from the first fractionating column 101, and outputting first refined product thereof;

[0121] The second hydrofining reactor 103 is provided with a material inlet for feeding in the first refined product from the first hydrofining reactor 102 and performing second hydrofining thereon, and outputting second refined product thereof as refined product thereof;

[0122] The first separation device 104 is provided with a material inlet for feeding in the refined product from the second hydrofining reactor 103 and separating the same, discharging light components, and outputting coal direct liquefaction full distillate oil;

[0123] The preparation system further comprises, connected in sequence through pipelines, a third fractionating column 201, a third hydrofining reactor 202, a fourth hydrofining reactor 203, and a second separation device 204.

[0124] The third fractionating column 201 is provided with a material inlet for feeding in coal indirect liquefaction oil and fractionating the same, outputting light oil fraction and heavy oil fraction;

[0125] The third hydrofining reactor 202 is provided with a material inlet for feeding in hydrogen to perform first hydrofining on the light oil fraction from the third fractionating column 201, and outputting first refined product thereof;

[0126] The fourth hydrofining reactor 203 is provided with a material inlet for feeding in the first refined product from the third hydrofining reactor 202 and subjecting it to secondary hydrofining, and outputting its second refined product as its refined product;

[0127] The second separation device 204 is provided with a material inlet for feeding in the refined product from the fourth hydrofining reactor 203 and subjecting it to separation, discharging light components, and outputting coal indirect liquefaction full-range oil;

[0128] The preparation system further comprises a mixer (not shown in the figure) for mixing and blending the obtained coal direct liquefaction full-range oil and the obtained coal indirect liquefaction full-range oil to obtain mixed oil.

[0129] The preparation system further comprises a fifth fractionating column 3 for fractionating and cutting the obtained mixed oil, discharging light components, and outputting integrated general-purpose fuel.

[0130] In an embodiment, as shown in Figure 1 , 2 The preparation system further comprises a coal direct liquefaction reaction unit 106, which is provided at its top with a hydrogen inlet, at its middle with a feed inlet and an oil outlet, and at its bottom with a residue outlet, and is connected to the material inlet of the first fractionating column 101 through its oil outlet, for carrying out coal direct liquefaction reaction to prepare coal direct liquefaction oil by feeding in coal and hydrogen, outputting coal direct liquefaction oil through its oil outlet to the first fractionating column 101, and outputting residue through its residue outlet.

[0131] In an embodiment, as shown in Figure 1 , 2 The preparation system further comprises a circulating solvent hydrostabilization reactor 107, which is provided at its top with a hydrogen inlet, at its middle with an oil inlet, and at its bottom with a circulating solvent outlet, and is connected to the heavy oil fraction outlet of the first fractionating column 101 through its oil inlet, and to the feed inlet of the coal direct liquefaction reaction unit 106 through its circulating solvent outlet, for feeding in heavy oil fraction from the first fractionating column 101 as solvent, and carrying out hydrostabilization by feeding in hydrogen to obtain solvent oil, and outputting the obtained solvent oil as circulating solvent through its circulating solvent outlet to the coal direct liquefaction reaction unit 106.

[0132] In an embodiment, as shown in Figure 1 , 2As shown, the preparation system further comprises a Fischer-Tropsch synthesis reaction unit 206, which is provided with an air inlet and an oil outlet, and is connected to the material inlet of the third fractional column 201 through the oil outlet thereof, for preparing coal indirect liquefied oil by Fischer-Tropsch synthesis reaction using the input synthesis gas, and outputting the coal indirect liquefied oil to the third fractional column 201 through the oil outlet thereof.

[0133] In one embodiment, the present application employs a preparation system as shown in Figure 1 The process for preparing integrated general fuel by the preparation system as shown is as follows:

[0134] (1) The coal direct liquefied oil from the coal direct liquefaction reaction unit 106 is sent to the first fractional column 101 for fractionation, and then the obtained light fraction oil is sent to the first hydrofining reactor 102 and the second hydrofining reactor 103 in sequence for two times of hydrofining, and then the obtained refined product stream is sent to the first separation device 104 for separation, to discharge light components and obtain coal direct liquefied full-range oil;

[0135] The heavy fraction oil obtained by fractionating the coal direct liquefied oil is sent to the hydrostabilization reactor as solvent raw material for solvent hydrostabilization, to output the circulating solvent to the coal direct liquefaction reaction unit 106;

[0136] (2) The coal indirect liquefied oil from the Fischer-Tropsch synthesis reaction unit 206 is sent to the third fractional column 201 for fractionation, and then the obtained light fraction oil is sent to the third hydrofining reactor 202 and the fourth hydrofining reactor 203 in sequence for two times of hydrofining, and then the obtained refined product stream is sent to the second separation device 204 for separation, to discharge wax and obtain coal indirect liquefied full-range oil;

[0137] (3) The coal direct liquefied full-range oil obtained in step (1) is sent to the second fractional column 105 for fractionation cutting, to discharge naphtha and obtain coal direct liquefied product oil; the coal indirect liquefied full-range oil obtained in step (2) is sent to the fourth fractional column 205 for fractionation cutting, to discharge naphtha and obtain coal indirect liquefied product oil; and then the obtained coal direct liquefied product oil and the obtained coal indirect liquefied product oil are sent to a mixer for mixing and blending, to obtain integrated general fuel.

[0138] In one embodiment, the present application employs a preparation system as shown in Figure 2 The process for preparing integrated general fuel by the preparation system as shown is as follows:

[0139] (1) sending the coal direct liquefaction oil from the coal direct liquefaction reaction unit 106 to the first fraction column 101 for fractionation, then sending the obtained light fraction oil to the first hydrofining reactor 102 and the second hydrofining reactor 103 in sequence for two times of hydrofining, and then sending the obtained refined product stream to the first separation device 104 for separation, discharging light components, and obtaining coal direct liquefaction full-range oil;

[0140] The heavy fraction oil obtained by fractionating the coal direct liquefaction oil is sent to a hydrostabilization reactor as a solvent raw material for solvent hydrostabilization to output a circulating solvent to the coal direct liquefaction reaction unit 106;

[0141] (2) sending the coal indirect liquefaction oil from the Fischer-Tropsch synthesis reaction unit 206 to the third fraction column 201 for fractionation, then sending the obtained light fraction oil to the third hydrofining reactor 202 and the fourth hydrofining reactor 203 in sequence for two times of hydrofining, and then sending the obtained refined product stream to the second separation device 204 for separation, discharging waxes, and obtaining coal indirect liquefaction full-range oil;

[0142] (3) sending the coal direct liquefaction full-range oil obtained in step (1) and the coal indirect liquefaction full-range oil obtained in step (2) to a mixer for mixing and blending, and then sending the obtained mixed oil to the fifth fraction column 3 for fractionation and cutting, discharging naphtha, and obtaining integrated general fuel.

[0143] The integrated general fuel of the present application can simultaneously meet the main indexes of diesel and jet fuel, can be used for logistics supply and oil supply guarantee of equipment requiring diesel and jet fuel, can simplify oil delivery procedures, shorten supply time, and has other military effects.

[0144] The preparation method and preparation system of the integrated general fuel of the present application can prepare the aforementioned integrated general fuel by combining mixing and blending with fractionation and cutting, and the process is simple, only a hydrofining reactor needs to be provided in the preparation process, and a coal direct liquefaction hydro-upgrading reactor and a coal indirect liquefaction hydrocracking and pour point depressing reactor are not needed, which reduces equipment investment, shortens the preparation process, and reduces preparation cost. It is beneficial to production cost. The integrated general fuel can simultaneously meet the main indexes of diesel and jet fuel, can be used for logistics supply and oil supply guarantee of equipment requiring diesel and jet fuel, can simplify oil delivery procedures, shorten supply time, and has other military effects.

[0145] The present application will be further described below through specific examples and comparative examples.

[0146] The sources of the raw materials used in the following examples and comparative examples are as follows:

[0147] All raw materials used are conventional raw materials in the field, and the purity specifications used are analytically pure or chemically pure. Unless otherwise specified, they are all commercially available.

[0148] Coal direct liquefaction diesel is a diesel fraction obtained by direct liquefaction of coal and solvent, taken from the process of the million-ton-level coal direct liquefaction industrial demonstration unit of the State Energy Group (Ordos);

[0149] Coal indirect liquefaction diesel is a diesel fraction obtained by Fischer-Tropsch synthesis of hydrogen and carbon monoxide, and is taken from the coal indirect liquefaction unit of Ningxia Coal Industry of China National Energy Group;

[0150] The physical and chemical properties of the raw material coal direct liquefaction diesel, coal indirect liquefaction diesel and the integrated universal fuel obtained by the present invention are specifically shown in Table 1.

[0151] Table 1 Physical and chemical properties of raw coal direct liquefaction diesel, coal indirect liquefaction diesel and the integrated universal fuel obtained by the present invention

[0152]

[0153]

[0154] Example 1

[0155] Use Figure 1 The preparation method and preparation system shown are used to prepare the integrated universal fuel G1, specifically including:

[0156] (1) The coal direct liquefaction oil from the coal direct liquefaction reaction unit 106 is sent to the first fractionation tower 101 for fractionation, and then the obtained light distillate oil is sent to the first hydrotreating reactor 102 and the second hydrotreating reactor 103 in sequence for two hydrotreating treatments, and then the obtained refined product stream is sent to the first separation device 104 for separation, and the light components are discharged to obtain the coal direct liquefaction full distillate oil;

[0157] The heavy distillate oil obtained by fractionation of the direct coal liquefaction oil is sent to the hydrogenation stabilization reactor as a solvent raw material for solvent hydrogenation stabilization, so as to output the circulating solvent to the direct coal liquefaction reaction unit 106;

[0158] (2) sending the coal indirect liquefaction oil from the Fischer-Tropsch synthesis reaction unit 206 to the third fractionation tower 201 for fractionation, and then sending the obtained light distillate oil to the third hydrotreating reactor 202 and the fourth hydrotreating reactor 203 in sequence for two hydrotreating treatments, and then sending the obtained refined product stream to the second separation device 204 for separation, discharging wax, and obtaining coal indirect liquefaction full distillate oil;

[0159] (3) First, the coal direct liquefaction full-fraction oil obtained in step (1) is sent to the second fractionating tower 105 for fractionation and cutting, and naphtha is discharged to obtain coal direct liquefaction product oil; the coal indirect liquefaction full-fraction oil obtained in step (2) is sent to the fourth fractionating tower 205 for fractionation and cutting, and naphtha is discharged to obtain coal indirect liquefaction product oil; then the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil are sent to a mixer for mixing and blending to obtain an integrated universal fuel; wherein,

[0160] In step (1), the distillation temperature of the coal direct liquefaction oil in the first distillation tower 101 is 320°C;

[0161] In step (1), the hydrotreating catalyst used in the hydrotreating is FFT-1, which specifically comprises:

[0162] The catalyst carrier is amorphous alumina;

[0163] Ni content is 6wt%, Mo content is 20wt%;

[0164] In step (1), the reaction temperature of the hydrofining is 380°C, the reaction pressure is 13.0 MPa, and the volume space velocity is 1.5 h -1 , hydrogen-to-oil ratio is 800V / V;

[0165] In step (2), the fractionation temperature of the CIL in the third fractionation tower 201 is 350° C.

[0166] In step (2), the hydrotreating catalyst used in the hydrotreating is FZC-3, which specifically comprises:

[0167] The catalyst carrier is amorphous alumina;

[0168] Ni content is 4wt%, Mo content is 15wt%;

[0169] In step (2), the reaction temperature of the hydrofining is 300°C, the reaction pressure is 8.0 MPa, and the volume space velocity is 1.0 h -1 , hydrogen-to-oil ratio is 300V / V;

[0170] In step (3), when the coal direct liquefaction full distillate oil obtained in step (1) is fractionated and cut in the second fractionating tower 105, the fractionation temperature is 180-270°C, that is, the lower limit of the fractionation temperature is 180°C and the upper limit is 270°C;

[0171] In step (3), when the coal indirect liquefaction full distillate oil obtained in step (2) is fractionated and cut in the fourth fractionating tower 205, the fractionation temperature is 160 to 300° C., that is, the lower limit of the fractionation temperature is 160° C. and the upper limit is 300° C.;

[0172] In step (3), the blending ratio of the obtained direct coal liquefaction product oil and the obtained indirect coal liquefaction product oil is 3:7 by mass ratio.

[0173] Example 2

[0174] Use Figure 1 The preparation method and system shown are used to prepare the integrated universal fuel G2, which differs from Example 1 only in that:

[0175] In step (1), the reaction temperature of the hydrofining is 350°C, the reaction pressure is 10.0 MPa, and the volume space velocity is 1.0 h -1 , hydrogen-to-oil ratio is 1000V / V;

[0176] In step (2), the fractionation temperature of the coal indirect liquefied oil in the third fractionation tower 201 is 320°C;

[0177] In step (3), when the coal indirect liquefaction full distillate oil obtained in step (2) is fractionated and cut in the fourth fractionating tower 205, the fractionation temperature is 170-280° C., that is, the lower limit of the fractionation temperature is 170° C. and the upper limit is 280° C.;

[0178] In step (3), the blending ratio of the obtained direct coal liquefaction product oil and the obtained indirect coal liquefaction product oil is 7:3 by mass ratio.

[0179] Example 3

[0180] Use Figure 2 The preparation method and preparation system shown are used to prepare the integrated universal fuel G3, specifically including:

[0181] (1) The coal direct liquefaction oil from the coal direct liquefaction reaction unit 106 is sent to the first fractionation tower 101 for fractionation, and then the obtained light distillate oil is sent to the first hydrotreating reactor 102 and the second hydrotreating reactor 103 in sequence for two hydrotreating treatments, and then the obtained refined product stream is sent to the first separation device 104 for separation, and the light components are discharged to obtain the coal direct liquefaction full distillate oil;

[0182] The heavy distillate oil obtained by fractionation of the direct coal liquefaction oil is sent to the hydrogenation stabilization reactor as a solvent raw material for solvent hydrogenation stabilization, so as to output the circulating solvent to the direct coal liquefaction reaction unit 106;

[0183] (2) the coal indirect liquefaction oil from the Fischer-Tropsch synthesis reaction unit 206 is sent to the third fraction column 201 for fractionation, and then the obtained light fraction oil is sent to the third hydrofining reactor 202 and the fourth hydrofining reactor 203 in sequence for two times of hydrofining, and then the obtained refined product stream is sent to the second separation device 204 for separation, and wax is discharged and coal indirect liquefaction full-range oil is obtained;

[0184] (3) the coal direct liquefaction full-range oil obtained in step (1) and the coal indirect liquefaction full-range oil obtained in step (2) are sent to a mixer for mixing and blending first, and then the obtained mixed oil is sent to the fifth fraction column 3 for fractionation cutting, and naphtha is discharged and integrated general fuel is obtained; wherein,

[0185] In step (1), the fractionation temperature of the coal direct liquefaction oil in the first fraction column 101 is 350°C;

[0186] In step (1), the hydrofining catalyst used for hydrofining is FFT-1B, which specifically comprises:

[0187] The catalyst carrier uses amorphous alumina;

[0188] The content of Ni is 4wt%, and the content of Mo is 15wt%;

[0189] In step (1), the reaction temperature of hydrofining is 380°C, the reaction pressure is 13.0MPa, the volume space velocity is 1.5h -1 , and the hydrogen / oil ratio is 800V / V;

[0190] In step (2), the fractionation temperature of the coal indirect liquefaction oil in the third fraction column 201 is 350°C;

[0191] In step (2), the hydrofining catalyst used for hydrofining comprises FZC-3, which specifically comprises:

[0192] The catalyst carrier uses amorphous alumina;

[0193] The content of Ni is 4wt%, and the content of Mo is 15wt%;

[0194] In step (2), the reaction temperature of hydrofining is 300°C, the reaction pressure is 8.0MPa, the volume space velocity is 1.0h -1 , and the hydrogen / oil ratio is 300V / V;

[0195] In step (3), the blending ratio of the coal direct liquefaction full-range oil obtained in step (1) and the coal indirect liquefaction full-range oil obtained in step (2) is 3:7 in terms of mass ratio;

[0196] In step (3), when the obtained mixed oil is fractionated and cut in the fifth fractionating tower 3, the fractionation temperature is 170-300°C, that is, the lower limit of the fractionation temperature is 170°C and the upper limit is 300°C.

[0197] Example 4

[0198] Use Figure 2 The preparation method and system shown are used to prepare the integrated universal fuel G4, which differs from Example 3 only in that:

[0199] In step (1), the distillation temperature of the coal direct liquefaction oil in the first distillation tower 101 is 320°C;

[0200] In step (1), the reaction temperature of the hydrofining is 350°C, the reaction pressure is 10.0 MPa, and the volume space velocity is 1.0 h -1 , hydrogen-to-oil ratio is 1000V / V;

[0201] In step (2), the fractionation temperature of the coal indirect liquefied oil in the third fractionation tower 201 is 320°C;

[0202] In step (3), the blending ratio of the coal direct liquefaction whole distillate oil obtained in step (1) and the coal indirect liquefaction whole distillate oil obtained in step (2) is 7:3 by mass;

[0203] In step (3), when the obtained mixed oil is fractionated and cut in the fifth fractionating tower 3, the fractionation temperature is 160-270°C, that is, the lower limit of the fractionation temperature is 160°C and the upper limit is 270°C.

[0204] Example 5

[0205] Use Figure 2 The preparation method and preparation system shown are used to prepare the integrated universal fuel G5, which differs from Example 3 only in that:

[0206] In step (1), the distillation temperature of the coal direct liquefaction oil in the first distillation tower 101 is 320°C;

[0207] In step (1), the reaction temperature of the hydrofining is 350°C, the reaction pressure is 13.0 MPa, and the volume space velocity is 1.5 h -1 , hydrogen-to-oil ratio is 800V / V;

[0208] In step (2), the fractionation temperature of the coal indirect liquefied oil in the third fractionation tower 201 is 320°C;

[0209] In step (2), the reaction temperature of the hydrofining is 300°C, the reaction pressure is 10.0 MPa, and the volume space velocity is 1.5 h -1 , hydrogen-to-oil ratio is 300V / V;

[0210] In step (3), the blending ratio of the coal direct liquefaction full distillate oil obtained in step (1) and the coal indirect liquefaction full distillate oil obtained in step (2) is 5:5 in terms of mass ratio;

[0211] In step (3), when the obtained mixed oil is subjected to fractionation cutting in the fifth fractionating column 3, the fractionation temperature is 170-280°C, that is, the lower limit of the fractionation temperature is 170°C and the upper limit is 280°C.

[0212] The physicochemical properties of the integrated general fuel G1, G2, G3, G4, G5 obtained in Examples 1-5 and the raw material coal direct liquefaction diesel oil and the coal indirect liquefaction diesel oil were tested, and the test results are shown in Table 2.

[0213] Table 2 Test results of physicochemical properties

[0214]

[0215] According to the examples and Tables 1-2, the integrated general fuel of the present application can simultaneously meet the main indexes of diesel oil and jet fuel;

[0216] The preparation method and preparation system of the integrated general fuel of the present application can prepare the aforementioned integrated general fuel by combining blending and fractionation cutting, and the process is simple, only a hydrogenation refining reactor is needed in the preparation process, and no coal direct liquefaction hydrogenation modification reactor and coal indirect liquefaction hydrogenation cracking and pour point depressing reactor are needed, which reduces the equipment investment, shortens the preparation process and reduces the preparation cost.

Claims

1. A method for preparing an integrated universal fuel, characterized in that: The indicators of the integrated universal fuel are as follows: The density at 20 ℃ is 0.775-0.830 g / cm 3 ; Freezing point ≤ -47 ℃; Net calorific value ≥42.8 MJ / Kg; Cetane number ≥45; Freezing point ≤ -50 ℃; Cold filter point ≤-50 ℃; Closed cup flash point ≥50 ℃; PAH content ≤ 1 wt%; 10% recovery temperature ≤ 205 ℃; 50% recovery temperature ≤ 232 ℃; Final distillation point ≤300℃; The preparation method comprises the following steps: (1) fractionating the coal direct liquefaction oil, then hydrotreating the obtained light distillate oil, and then separating the obtained refined product stream to obtain the coal direct liquefaction full distillate oil; wherein, The fractionation temperature of coal direct liquefaction oil is 300~350℃; (2) fractionating the CIL oil, then hydrotreating the resulting light distillate oil, and then separating the resulting refined product stream to obtain CIL full distillate oil; wherein, The fractionation temperature of coal indirect liquefaction oil is 320~350℃; (3) fractionating and cutting the coal direct liquefaction full-fraction oil obtained in step (1) and the coal indirect liquefaction full-fraction oil obtained in step (2) in any order and mixing and blending to obtain an integrated universal fuel; wherein, In step (3), the coal direct liquefaction full-fraction oil obtained in step (1) and the coal indirect liquefaction full-fraction oil obtained in step (2) are first fractionated and cut respectively to discharge the light components, and obtain the coal direct liquefaction product oil and the coal indirect liquefaction product oil; then the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil are mixed and blended to obtain an integrated universal fuel; and in step (3), when the coal direct liquefaction full-fraction oil obtained in step (1) is fractionated and cut, the lower limit of the fractionation temperature is 150-180°C and the upper limit is 260-300°C; in step (3), when the coal indirect liquefaction full-fraction oil obtained in step (2) is fractionated and cut, the lower limit of the fractionation temperature is 150-180°C and the upper limit is 260-300°C; in step (3), the blending ratio of the obtained coal direct liquefaction product oil and the obtained coal indirect liquefaction product oil is 1:9~9:1 according to the mass ratio; or, In step (3), the whole distillate oil obtained from direct coal liquefaction in step (1) and the whole distillate oil obtained from indirect coal liquefaction in step (2) are first mixed and blended; then the obtained mixed oil is fractionated and cut to discharge the light components to obtain an integrated universal fuel; and in step (3), the blending ratio of the whole distillate oil obtained from direct coal liquefaction in step (1) and the whole distillate oil obtained from indirect coal liquefaction in step (2) is 1:9 to 9:1 in terms of mass ratio; in step (3), when the obtained mixed oil is fractionated and cut, the lower limit of the fractionation temperature is 150-180°C and the upper limit is 260-300°C.

2. The preparation method according to claim 1, characterized in that In step (1), the reaction temperature of the hydrofining is 320-400 °C, and / or the reaction pressure is 6.0-20.0 MPa, and / or the volume space velocity is 0.5-4.0 h -1 , and / or hydrogen to oil ratio of 500-1500 V / V.

3. The preparation method according to claim 1, characterized in that In step (2), the reaction temperature of the hydrofining is 300-350 °C, and / or the reaction pressure is 5.0-10.0 MPa, and / or the volume space velocity is 0.5-4.0 h -1 , and / or a hydrogen-to-oil ratio of 200-800 V / V.

4. The preparation method according to any one of claims 1 to 3, characterized in that In step (1), hydrofining is performed twice continuously; and / or, In step (1), the coal direct liquefaction oil is a coal direct liquefaction oil obtained by direct liquefaction of coal; and / or, In step (2), hydrofining is performed twice continuously; and / or, In step (2), the coal indirect liquefaction oil is the coal indirect liquefaction oil produced by the Fischer-Tropsch synthesis reaction of synthesis gas.

5. An integrated universal fuel prepared according to the preparation method according to any one of claims 1 to 4.

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