System and method for producing gasoline, diesel and kerosene

Abstract

The invention provides a system and a method for producing gasoline, diesel oil and kerosene, an outlet of an indirect liquefied oil supply storage tank is connected with an inlet of an indirect liquefied oil treatment unit, the indirect liquefied oil is subjected to hydrocracking and isomerization reaction in the indirect liquefied oil treatment unit, and rectification separation is carried out; a gasoline fraction A, a diesel fraction A, a first fraction and a diesel fraction B are obtained; an outlet of an MTP byproduct mixed aromatic hydrocarbon supply storage tank is connected with an inlet of an MTP byproduct mixed aromatic hydrocarbon treatment unit, the MTP byproduct mixed aromatic hydrocarbon is subjected to aromatization and isomerization reaction and rectification separation, and a gasoline fraction B and a diesel fraction C are obtained; carrying out hydrofining reaction and rectification separation on the MTP byproduct mixed aromatic hydrocarbon to obtain a gasoline fraction C and a kerosene fraction; the produced fractions are introduced into a blending unit to be subjected to combined processing treatment, indexes are complementary, the product quality is improved, and gasoline, diesel oil and kerosene meeting the national standard are obtained.

Description

Technical Field

[0001] The present invention relates to the field of coal chemical industry, and in particular to a system and method for producing gasoline, diesel and kerosene. Background Art

[0002] The indirect liquefied oil obtained by hydrogenation of Fischer-Tropsch oil (wax) is mainly composed of normal alkanes and isoalkanes, with very few aromatics and cycloalkanes. This results in the gasoline fraction prepared from the indirect liquefied oil having a low octane number, and the kerosene fraction and diesel fraction having low density and poor lubricity. Therefore, it is impossible to directly produce high-quality gasoline, diesel and kerosene of qualified quality from the indirect liquefied oil.

[0003] The MTP byproduct mixed aromatics produced in the methanol to propylene process can also be used to produce gasoline, but the MTP byproduct mixed aromatics are mainly composed of olefins, alkanes, cycloalkanes and aromatics, with an octane number of >95%. Due to its high olefin content and a certain amount of dienes, the oxidation stability and gum content are unqualified. In addition, the olefin or aromatic content exceeds the standard, resulting in low quality and unqualified quality of the prepared gasoline, and it is also impossible to prepare high-quality diesel and kerosene of qualified quality.

[0004] In summary, the prior art uses indirect liquefied oil and / or MTP by-product mixed aromatics, and is unable to produce high-quality gasoline, diesel and kerosene of acceptable quality.

[0005] In view of this, this application is hereby filed. Summary of the invention

[0006] The main purpose of the present invention is to provide a system and method for producing gasoline, diesel and kerosene to solve the problem in the prior art that high-quality gasoline, diesel and kerosene of qualified quality cannot be produced from indirect liquefied oil and / or MTP by-product mixed aromatics.

[0007] To achieve the above object, according to one aspect of the present invention, there is provided a system for producing gasoline, diesel and kerosene, comprising: a raw material supply unit, the raw material supply unit comprising an indirect liquefied oil supply storage tank and an MTP by-product mixed aromatics supply storage tank (10);

[0008] An indirect liquefied oil processing unit, the indirect liquefied oil processing unit comprises a first atmospheric distillation tower (1), a first vacuum distillation tower (2), a hydrocracking and isomerization reactor (3), a second atmospheric distillation tower (4) and a second vacuum distillation tower (5) which are connected in sequence; wherein the inlet of the first atmospheric distillation tower (1) is connected to the outlet of the indirect liquefied oil supply tank, the first atmospheric distillation tower (1) has a first atmospheric tower bottom outlet, the first atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower (2), the first vacuum distillation tower (2) The first vacuum tower bottom outlet is connected to the inlet of the hydrocracking and isomerization reactor (3), the outlet of the hydrocracking and isomerization reactor (3) is connected to the inlet of the second atmospheric distillation tower (4), the second atmospheric distillation tower (4) has a second atmospheric tower top outlet, a second atmospheric first side line outlet, a second atmospheric second side line outlet and a second atmospheric tower bottom outlet, the second atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower (5), and the second vacuum distillation tower (5) has a second vacuum first side line outlet;

[0009] The MTP by-product mixed aromatic hydrocarbons processing unit comprises an aromatization and isomerization reactor (6), a first mixed aromatic hydrocarbons distillation tower (7), a hydrotreating reactor (8) and a second mixed aromatic hydrocarbons distillation tower (9); wherein the inlet of the aromatization and isomerization reactor (6) is connected to the outlet of the MTP by-product mixed aromatic hydrocarbons supply storage tank (10), the outlet of the aromatization and isomerization reactor (6) is connected to the inlet of the first mixed aromatic hydrocarbons distillation tower (7), and the first mixed aromatic hydrocarbons distillation tower (7) has a first mixed aromatic hydrocarbons tower top outlet and a first mixed aromatic hydrocarbons tower bottom outlet; the inlet of the hydrotreating reactor (8) is connected to the outlet of the MTP by-product mixed aromatic hydrocarbons supply storage tank (10), the outlet of the hydrotreating reactor (8) is connected to the inlet of the second mixed aromatic hydrocarbons distillation tower (9), and the second mixed aromatic hydrocarbons distillation tower (9) has a second mixed aromatic hydrocarbons tower top outlet and a second mixed aromatic hydrocarbons tower bottom outlet;

[0010] A blending unit, the blending unit comprising a diesel blending kettle (100), a gasoline blending kettle (200) and a kerosene blending kettle (300); the diesel blending kettle (100) has a first diesel inlet, a second diesel inlet, a third diesel inlet and a fourth diesel inlet, the second normal pressure first side line outlet is connected to the first diesel inlet of the diesel blending kettle (100), the second normal pressure second side line outlet is connected to the second diesel inlet of the diesel blending kettle (100), the second reduced pressure first side line outlet is connected to the third diesel inlet of the diesel blending kettle (100), and the first mixed aromatic tower bottom outlet is connected to the fourth diesel inlet of the diesel blending kettle (100); The gasoline blending kettle (200) has a first gasoline inlet, a second gasoline inlet and a third gasoline inlet, the second atmospheric tower top outlet is connected to the first gasoline inlet of the gasoline blending kettle (200), the first mixed aromatic tower top outlet is connected to the second gasoline inlet of the gasoline blending kettle (200); the second mixed aromatic tower top outlet is connected to the third gasoline inlet of the gasoline blending kettle (200); the kerosene blending kettle (300) has a first kerosene inlet and a second kerosene inlet, the second atmospheric first side line outlet is connected to the first kerosene inlet of the kerosene blending kettle (300), and the second mixed aromatic tower bottom outlet is connected to the second kerosene inlet of the kerosene blending kettle (300).

[0011] Furthermore, the first atmospheric distillation tower (1) also has a first atmospheric tower top outlet, a first atmospheric first side line outlet and a first atmospheric second side line outlet, and the first atmospheric first side line outlet is higher than the first atmospheric second side line outlet.

[0012] Furthermore, the first vacuum distillation tower (2) also has a first vacuum first side line outlet, a first vacuum second side line outlet and a first vacuum third side line outlet; the first vacuum first side line outlet is higher than the first vacuum second side line outlet, and the first vacuum second side line outlet is higher than the first vacuum third side line outlet.

[0013] Furthermore, the second atmospheric pressure first side line outlet of the second atmospheric pressure distillation tower (4) is higher than the second atmospheric pressure second side line outlet.

[0014] Furthermore, the second vacuum distillation tower (5) also has a second vacuum second side line outlet, a second vacuum third side line outlet and a second vacuum tower bottom outlet; the second vacuum first side line outlet is higher than the second vacuum second side line outlet, and the second vacuum second side line outlet is higher than the second vacuum third side line outlet.

[0015] Furthermore, a first valve is provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle (300).

[0016] Furthermore, a second valve is provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle (100).

[0017] Furthermore, a third valve is provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle (100).

[0018] Furthermore, a fourth valve is provided on the pipeline connecting the MTP by-product mixed aromatic hydrocarbon supply storage tank (10) and the aromatization and isomerization reactor (6).

[0019] Furthermore, a fifth valve is provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the hydrotreating reactor (8).

[0020] Furthermore, the diesel blending kettle (100) has a diesel outlet at its bottom.

[0021] Furthermore, the gasoline blending kettle (200) has a gasoline outlet at the bottom thereof.

[0022] Furthermore, the bottom of the kerosene blending kettle (300) is provided with a kerosene outlet.

[0023] Furthermore, the kerosene blending kettle (300) also has an additive inlet, and the additive inlet is used to provide additives to the kerosene blending kettle (300).

[0024] According to another aspect of the present invention, a method for producing gasoline, diesel and kerosene is provided, the method comprising the following steps: step S1, subjecting the indirect liquefied oil to a first atmospheric distillation separation to obtain a ≥C18 hydrocarbon mixture; subjecting the ≥C18 hydrocarbon mixture to a first vacuum distillation separation to obtain a ≥C40 hydrocarbon mixture; subjecting the ≥C40 hydrocarbon mixture to a hydrocracking reaction and an isomerization reaction to obtain a first product; subjecting the first product to a second atmospheric distillation separation to obtain a gasoline fraction A, a side fraction and a second atmospheric tower bottom fraction, the side fraction comprising a diesel fraction A and / or a first fraction, the gasoline fraction A being a C5-C10 hydrocarbon mixture, the first fraction A being a C10-C14 hydrocarbon mixture, the diesel fraction A being a C10-C16 hydrocarbon mixture, and the second atmospheric tower bottom fraction being a ≥C16 hydrocarbon mixture; subjecting the ≥C16 hydrocarbon mixture to a second vacuum distillation separation to obtain a diesel fraction B, the diesel fraction B being a C16-C21 hydrocarbon mixture;

[0025] Step S2, performing aromatization reaction and isomerization reaction on the MTP by-product mixed aromatics to obtain a second product; performing a first mixed aromatic distillation separation on the second product to obtain a gasoline fraction B and a diesel fraction C; the gasoline fraction B is a C5-C12 hydrocarbon mixture, and the diesel fraction C is a ≥C12 hydrocarbon mixture; performing a hydrofining reaction on the MTP by-product mixed aromatics to obtain a third product; performing a second mixed aromatic distillation separation on the third product to obtain a gasoline fraction C and a kerosene fraction; the gasoline fraction is a C5-C8 hydrocarbon mixture, and the kerosene fraction is a ≥C8 hydrocarbon mixture;

[0026] Step S3, mixing diesel fraction A, diesel fraction B and diesel fraction C to obtain diesel; mixing gasoline fraction A and gasoline intermediate to obtain gasoline; wherein the gasoline intermediate includes gasoline fraction B and / or gasoline fraction C; mixing kerosene fraction and the first fraction to obtain kerosene;

[0027] The indirect liquefied oil includes 80-90wt% normal alkanes, 9-19wt% isoalkanes, 0.01-1wt% aromatics and 0.01-1wt% cycloalkanes; the MTP by-product mixed aromatics include 30-50wt% monoolefins, 1-10wt% diolefins, 20-30wt% alkanes, 9-20wt% cycloalkanes and 20-40wt% aromatics.

[0028] Furthermore, in step S1, the temperature of the first atmospheric distillation separation is 250-500°C, and the pressure of the first atmospheric distillation separation is 0.05-2.0 MPa.

[0029] Furthermore, the temperature of the first vacuum distillation separation is 200-400° C., and the pressure of the first vacuum distillation separation is 0-0.1 MPa.

[0030] Furthermore, the conditions for the hydrocracking reaction and the isomerization reaction include: a temperature of 280 to 450° C., a pressure of 6 to 13 MPa, a volume space velocity of 1 to 3.5 hl, and a hydrogen-to-oil volume ratio of 400 to 800:1.

[0031] Furthermore, the temperature of the second atmospheric distillation separation is 250-400° C., and the pressure of the second atmospheric distillation separation is 0.1-1.0 MPa.

[0032] Furthermore, the temperature of the second vacuum distillation separation is 200-350° C., and the pressure of the second vacuum distillation separation is 0-0.1 MPa.

[0033] Furthermore, in step S2, the conditions for the aromatization reaction and the isomerization reaction are: a temperature of 260 to 400° C. and a pressure of 0.8 to 1.1 MPa.

[0034] Furthermore, the temperature of the first mixed aromatic distillation separation is 250-300° C., and the pressure of the first mixed aromatic distillation separation is 0.1-1.0 MPa.

[0035] Furthermore, in step S2, the conditions for the hydrofining reaction are: temperature of 300-400°C, pressure of 4.5-9.5 MPa, and volume space velocity of 1-4 h -1 , the volume ratio of hydrogen to oil is 300-700:1.

[0036] Furthermore, the temperature of the second mixed aromatic distillation separation is 120-200° C., and the pressure of the second mixed aromatic distillation separation is 0.1-1.0 MPa.

[0037] Furthermore, in step S3, the volume ratio of diesel fraction A, diesel fraction B and diesel fraction C is 1:0.01-1:0.6-1.

[0038] Furthermore, the volume ratio of the gasoline fraction A to the gasoline intermediate is 1:1-2.

[0039] Furthermore, the volume ratio of the first fraction to the kerosene fraction is 1:1-3.

[0040] Furthermore, in step S3, the kerosene also includes additives.

[0041] Furthermore, the additive is an antistatic agent.

[0042] Furthermore, the dosage of the additive is 1 to 3 mg / L.

[0043] The technical scheme of the present invention is applied to the system for producing gasoline, diesel and kerosene provided by the present invention, wherein a first atmospheric distillation tower and a first vacuum distillation tower are used to distill and purify the indirect liquefied oil, and then a hydrocracking and hydroisomerization reactor is used to perform hydrocracking and hydroisomerization reactions, and then a second atmospheric distillation tower and a second vacuum distillation tower are used for separation to obtain a gasoline fraction A, a diesel fraction A, a first fraction and a diesel fraction B;

[0044] The olefins in the MTP by-product mixed aromatics are converted into aromatics or alkanes by aromatization and isomerization reactors, solving the problems of excessive olefins and diolefins, unqualified oxidation stability and colloid content in the MTP by-product mixed aromatics. The mixture is then separated by the first mixed aromatics distillation tower to obtain gasoline fraction B and diesel fraction C.

[0045] A hydrotreating reactor is used to convert olefins and most of the aromatics in the MTP by-product mixed aromatics into alkanes and cycloalkanes, solving the problem of high olefin and aromatic content in the MTP by-product mixed aromatics. The mixture is then separated through a second aromatic distillation tower to obtain gasoline fraction C and kerosene fraction.

[0046] The diesel fractions obtained by reacting and separating the indirect liquefied oil and the MTP by-product mixed aromatics are blended in a diesel blending kettle, thereby achieving the production of qualified diesel; the gasoline fractions are blended in a gasoline blending kettle, thereby achieving the production of qualified gasoline; the kerosene fraction and the first fraction are blended in a kerosene blending kettle, thereby achieving the production of qualified kerosene.

[0047] In summary, the system for producing gasoline, diesel and kerosene provided in the present application jointly processes the oil products produced by the two processing units of indirect liquefied oil and MTP by-product mixed aromatics, with complementary indicators and improved product quality, thereby being able to produce gasoline, diesel and kerosene that meet national standards with high economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0048] The drawings constituting a part of the present application are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0049] Figure 1 A system for producing gasoline, diesel and kerosene provided in one embodiment of the present invention is shown;

[0050] The above drawings include the following reference numerals:

[0051] 1. The first atmospheric distillation tower; 2. The first vacuum distillation tower; 3. The hydrocracking and isomerization reactor; 4. The second atmospheric distillation tower; 5. The second vacuum distillation tower; 6. The aromatization and isomerization reactor; 7. The first mixed aromatic distillation tower; 8. The hydrofining reactor; 9. The second mixed aromatic distillation tower; 10. The MTP by-product mixed aromatics supply tank; 100. The diesel blending kettle; 200. The gasoline blending kettle; 300. The kerosene blending kettle. DETAILED DESCRIPTION

[0052] It should be noted that, in the absence of conflict, the embodiments and features in the embodiments of the present application can be combined with each other. The present invention will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0053] As analyzed in the background of this application, the prior art has the problem that it is impossible to produce high-quality gasoline, diesel and kerosene with qualified quality from indirect liquefied oil and / or MTP by-product mixed aromatics. In order to solve this problem, this application provides a system and method for producing gasoline, diesel and kerosene.

[0054] In a typical embodiment of the present application, a system for producing gasoline, diesel and kerosene is provided, such as Figure 1 As shown, the system comprises: a raw material supply unit, the raw material supply unit comprises an indirect liquefied oil supply storage tank (not shown in the figure) and an MTP by-product mixed aromatics supply storage tank (10); the indirect liquefied oil supply storage tank is used to store indirect liquefied oil, and the MTP by-product mixed aromatics supply storage tank (10) is used to store MTP by-product mixed aromatics;

[0055] The indirect liquefied oil processing unit comprises a first atmospheric distillation tower (1), a first vacuum distillation tower (2), a hydrocracking and isomerization reactor (3), a second atmospheric distillation tower (4) and a second vacuum distillation tower (5) which are connected in sequence; wherein:

[0056] The inlet of the first atmospheric distillation tower (1) is connected to the outlet of the indirect liquefied oil supply storage tank, the first atmospheric distillation tower (1) has a first atmospheric tower bottom outlet, the first atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower (2), the first vacuum distillation tower (2) has a first vacuum tower bottom outlet, the first vacuum tower bottom outlet is connected to the inlet of the hydrocracking and isomerization reactor (3), the outlet of the hydrocracking and isomerization reactor (3) is connected to the inlet of the second atmospheric distillation tower (4), the second atmospheric distillation tower (4) has a second atmospheric tower top outlet, a second atmospheric first side line outlet, a second atmospheric second side line outlet and a second atmospheric tower bottom outlet, the second atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower (5), and the second vacuum distillation tower (5) has a second vacuum first side line outlet;

[0057] An MTP by-product mixed aromatics processing unit, the MTP by-product mixed aromatics processing unit comprising an aromatization and isomerization reactor (6), a first mixed aromatics distillation tower (7), a hydrotreating reactor (8) and a second mixed aromatics distillation tower (9);

[0058] The inlet of the aromatization and isomerization reactor (6) is connected to the outlet of the MTP by-product mixed aromatic hydrocarbon supply storage tank (10), and the outlet of the aromatization and isomerization reactor (6) is connected to the inlet of the first mixed aromatic distillation tower (7), and the first mixed aromatic distillation tower (7) has a first mixed aromatic tower top outlet and a first mixed aromatic tower bottom outlet;

[0059] The inlet of the hydrotreating reactor (8) is connected to the outlet of the MTP by-product mixed aromatic hydrocarbon supply storage tank (10), and the outlet of the hydrotreating reactor (8) is connected to the inlet of the second mixed aromatic distillation tower (9), and the second mixed aromatic distillation tower (9) has a second mixed aromatic tower top outlet and a second mixed aromatic tower bottom outlet;

[0060] A blending unit, the blending unit comprising a diesel blending kettle (100), a gasoline blending kettle (200) and a kerosene blending kettle (300);

[0061] The diesel blending kettle (100) has a first diesel inlet, a second diesel inlet, a third diesel inlet and a fourth diesel inlet, the second normal pressure first side line outlet is connected to the first diesel inlet of the diesel blending kettle (100), the second normal pressure second side line outlet is connected to the second diesel inlet of the diesel blending kettle (100), the second reduced pressure first side line outlet is connected to the third diesel inlet of the diesel blending kettle (100), and the first mixed aromatic tower bottom outlet is connected to the fourth diesel inlet of the diesel blending kettle (100);

[0062] The gasoline blending kettle (200) has a first gasoline inlet, a second gasoline inlet and a third gasoline inlet; the second atmospheric tower top outlet is connected to the first gasoline inlet of the gasoline blending kettle (200); the first mixed aromatic tower top outlet is connected to the second gasoline inlet of the gasoline blending kettle (200); and the second mixed aromatic tower top outlet is connected to the third gasoline inlet of the gasoline blending kettle (200);

[0063] The kerosene blending kettle (300) has a first kerosene inlet and a second kerosene inlet, the second normal pressure first side line outlet is connected to the first kerosene inlet of the kerosene blending kettle (300), and the second mixed aromatic tower bottom outlet is connected to the second kerosene inlet of the kerosene blending kettle (300).

[0064] The system for producing gasoline, diesel and kerosene provided by the present invention adopts a first atmospheric distillation tower and a first vacuum distillation tower to distill and purify the indirect liquefied oil, and then adopts a hydrocracking and isomerization reactor to carry out hydrocracking reaction and hydroisomerization reaction, and then separates through a second atmospheric distillation tower and a second vacuum distillation tower to obtain a gasoline fraction A, a diesel fraction A, a first fraction and a diesel fraction B;

[0065] The olefins in the MTP by-product mixed aromatics are converted into aromatics or alkanes by aromatization and isomerization reactors, solving the problems of excessive monoolefins and diolefins, unqualified oxidation stability and colloid content in the MTP by-product mixed aromatics. The products are then separated by the first mixed aromatics distillation tower to obtain gasoline fraction B and diesel fraction C.

[0066] A hydrotreating reactor is used to convert olefins and most of the aromatics in the MTP by-product mixed aromatics into alkanes and cycloalkanes, solving the problem of high olefin and aromatic content in the MTP by-product mixed aromatics. The mixture is then separated through a second aromatic distillation tower to obtain gasoline fraction C and kerosene fraction.

[0067] The diesel fractions obtained by reacting and separating the indirect liquefied oil and the MTP by-product mixed aromatics are blended in a diesel blending kettle, thereby achieving the production of qualified diesel; the gasoline fractions are blended in a gasoline blending kettle, thereby achieving the production of qualified gasoline; the kerosene fraction and the first fraction are blended in a kerosene blending kettle, thereby achieving the production of qualified kerosene.

[0068] In summary, the system for producing gasoline, diesel and kerosene provided in the present application jointly processes the oil products produced by the two processing units of indirect liquefied oil and MTP by-product mixed aromatics, with complementary indicators and improved product quality, thereby being able to produce gasoline, diesel and kerosene that meet national standards with high economic benefits.

[0069] In some embodiments, the first atmospheric distillation tower (1) further comprises a first atmospheric tower top outlet, a first atmospheric pressure first side line outlet and a first atmospheric pressure second side line outlet, wherein the first atmospheric pressure first side line outlet is higher than the first atmospheric pressure second side line outlet; the first atmospheric pressure tower top outlet is used to discharge a C5-C10 hydrocarbon mixture, the first atmospheric pressure first side line outlet is used to discharge a C10-C14 hydrocarbon mixture, and the first atmospheric pressure second side line outlet is used to discharge a C14-C18 hydrocarbon mixture.

[0070] In some embodiments, the first vacuum distillation tower (2) further has a first vacuum first side line outlet, a first vacuum second side line outlet and a first vacuum third side line outlet; the first vacuum first side line outlet is higher than the first vacuum second side line outlet, and the first vacuum second side line outlet is higher than the first vacuum third side line outlet; the first vacuum first side line outlet is used to discharge a C18-C21 hydrocarbon mixture, the first vacuum second side line outlet is used to discharge a C21-C25 hydrocarbon mixture, and the first vacuum third side line outlet is used to discharge a C25-C40 hydrocarbon mixture.

[0071] In some embodiments, the second atmospheric pressure first side line outlet of the second atmospheric distillation tower (4) is higher than the second atmospheric pressure second side line outlet; so as to obtain the first fraction and the diesel fraction A with higher purity.

[0072] In some embodiments, the second vacuum distillation tower (5) further has a second vacuum second side line outlet, a second vacuum third side line outlet and a second vacuum bottom outlet; the second vacuum first side line outlet is higher than the second vacuum second side line outlet, and the second vacuum second side line outlet is higher than the second vacuum third side line outlet; the second vacuum second side line outlet is used to discharge a C21-C25 hydrocarbon mixture, the second vacuum third side line outlet is used to discharge a C25-C40 hydrocarbon mixture, and the second vacuum bottom outlet is used to discharge a C40 hydrocarbon mixture.

[0073] In some embodiments, a first valve (not shown in the figure) is provided on the pipeline connecting the second normal pressure first side line outlet to the kerosene blending kettle (300) to control the on-off and flow rate of the first distillate discharged from the second normal pressure first side line outlet to the kerosene blending kettle (300). A second valve (not shown in the figure) is provided on the pipeline connecting the second normal pressure first side line outlet to the diesel blending kettle (100) to control the on-off and flow rate of the first distillate discharged from the second normal pressure first side line outlet to the diesel blending kettle (100). A third valve (not shown in the figure) is provided on the pipeline connecting the second normal pressure second side line outlet to the diesel blending kettle (100) to control the on-off and flow rate of the second distillate discharged from the second normal pressure second side line outlet to the diesel blending kettle (100). When preparing gasoline and kerosene, the first valve is opened, the second valve is closed, and the third valve is closed; when preparing gasoline and diesel, the first valve is closed, the second valve is opened, and the third valve is opened; when gasoline, kerosene and diesel are prepared at the same time, the first valve, the second valve and the third valve are all opened.

[0074] In some embodiments, a fourth valve (not shown in the figure) is provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the aromatization and isomerization reactor (6) to control the on-off and flow rate of the MTP by-product mixed aromatics to the aromatization and isomerization reactor (6); a fifth valve (not shown in the figure) is provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the hydrofining reactor (8) to control the on-off and flow rate of the MTP by-product mixed aromatics to the hydrofining reactor (8). When preparing gasoline and diesel, the fourth valve is opened and the fifth valve is closed; when preparing gasoline and kerosene, the fourth valve is closed and the fifth valve is opened; when preparing kerosene, diesel and gasoline at the same time, both the fourth valve and the fifth valve are opened.

[0075] In some embodiments, the diesel blending kettle (100) has a diesel outlet at the bottom to facilitate the discharge of diesel.

[0076] In some embodiments, the bottom of the gasoline blending kettle (200) has a gasoline outlet to facilitate the discharge of gasoline.

[0077] In some embodiments, the bottom of the kerosene blending kettle (300) has a kerosene outlet to facilitate the discharge of kerosene.

[0078] In some embodiments, the kerosene blending kettle (300) further has an additive inlet, which is used to provide additives to the kerosene blending kettle (300) to further improve the properties of the kerosene.

[0079] In some embodiments, the system further includes a plurality of flow meters for controlling the addition amount of each blending component in the preparation of kerosene, diesel or gasoline, so as to produce oil products with stable quality. A first flow meter (not shown in the figure) is provided on the pipeline connecting the second normal pressure first side line outlet with the first diesel inlet of the diesel blending kettle 100, a second flow meter (not shown in the figure) is provided on the pipeline connecting the second normal pressure second side line outlet with the second diesel inlet of the diesel blending kettle 100, a third flow meter (not shown in the figure) is provided on the pipeline connecting the second reduced pressure first side line outlet with the third diesel inlet of the diesel blending kettle 100; a fourth flow meter (not shown in the figure) is provided on the pipeline connecting the first mixed aromatic tower bottom outlet with the fourth diesel inlet of the diesel blending kettle 100;

[0080] A fifth flow meter (not shown in the figure) is provided on the pipeline connecting the top outlet of the second atmospheric tower with the first gasoline inlet of the gasoline blending kettle 200, a sixth flow meter (not shown in the figure) is provided on the pipeline connecting the top outlet of the first mixed aromatic tower with the second gasoline inlet of the gasoline blending kettle 200, and a seventh flow meter (not shown in the figure) is provided on the pipeline connecting the top outlet of the second mixed aromatic tower with the third gasoline inlet of the gasoline blending kettle 200;

[0081] An eighth flow meter (not shown in the figure) is arranged on the pipeline connecting the second normal pressure first side line outlet with the first kerosene inlet of the kerosene blending kettle 300, and a ninth flow meter (not shown in the figure) is arranged on the pipeline connecting the second mixed aromatic tower bottom outlet with the second kerosene inlet of the kerosene blending kettle 300.

[0082] In another typical embodiment of the present application, a method for producing gasoline, diesel and kerosene is provided, the method comprising the following steps: step S1, transporting the indirect liquefied oil from the indirect liquefied oil supply tank to a first atmospheric distillation tower (1) for first atmospheric distillation separation, and obtaining a ≥C18 hydrocarbon mixture from the bottom outlet of the first atmospheric distillation tower; transporting the ≥C18 hydrocarbon mixture to a first vacuum distillation tower (2) for first vacuum distillation separation, and obtaining a ≥C40 hydrocarbon mixture from the bottom outlet of the first vacuum distillation tower; transporting the ≥C40 hydrocarbon mixture to a hydrocracking and isomerization reactor (3) for hydrocracking reaction and isomerization reaction to obtain a first product; transporting the first product to a second atmospheric distillation tower (4) for second atmospheric distillation separation, and obtaining a ≥C18 hydrocarbon mixture from the bottom outlet of the first atmospheric distillation tower; A gasoline fraction A is obtained from the top outlet of the second atmospheric pressure tower, a first fraction is obtained from the first side line outlet of the second atmospheric pressure tower, a second fraction (C14-C16 hydrocarbon mixture) is obtained from the second side line outlet of the second atmospheric pressure tower, and a C16 hydrocarbon mixture is obtained from the bottom outlet of the second atmospheric pressure tower; the first fraction and the second fraction are mixed to form a diesel fraction A, the side line fraction includes the diesel fraction A and / or the first fraction, the gasoline fraction A is a C5-C10 hydrocarbon mixture, the first fraction is a C10-C14 hydrocarbon mixture, and the diesel fraction A is a C10-C16 hydrocarbon mixture; the C16 hydrocarbon mixture is transported to a second vacuum distillation tower (5) for second vacuum distillation separation, and a diesel fraction B is obtained from the second vacuum first side line outlet, and the diesel fraction B is a C16-C21 hydrocarbon mixture;

[0083] Step S2, transporting the MTP by-product mixed aromatics from the MTP by-product mixed aromatics supply storage tank (10) to an aromatization and isomerization reactor (6) for aromatization reaction and isomerization reaction to obtain a second product; transporting the second product to a first mixed aromatic distillation tower (7) for first mixed aromatic distillation separation, obtaining a gasoline fraction B from the top outlet of the first mixed aromatic tower, and obtaining a diesel fraction C from the bottom outlet of the first mixed aromatic tower; the gasoline fraction B is a C5-C12 hydrocarbon mixture, and the diesel fraction C is ≥ C12 hydrocarbon mixture; transporting the MTP by-product mixed aromatics from the MTP by-product mixed aromatics supply storage tank (10) to a hydrotreating reactor (8) for hydrotreating reaction to obtain a third product; transporting the third product to a second mixed aromatic distillation tower (9) for second mixed aromatic distillation separation, obtaining a gasoline fraction C from the top outlet of the second mixed aromatic tower, and obtaining a kerosene fraction from the bottom outlet of the second mixed aromatic tower; the gasoline fraction C is a C5-C8 hydrocarbon mixture, and the kerosene fraction is a C8 hydrocarbon mixture;

[0084] Step S3, mixing diesel fraction A, diesel fraction B and diesel fraction C to obtain diesel; mixing gasoline fraction A and gasoline intermediate to obtain gasoline; wherein the gasoline intermediate includes gasoline fraction B and / or gasoline fraction C; mixing kerosene fraction and the first fraction to obtain kerosene;

[0085] Among them, the indirect liquefied oil includes 80-90wt% normal alkanes, 9-19wt% isoalkanes, 0.01-1wt% aromatics and 0.01-1wt% cycloalkanes; the MTP by-product mixed aromatics include 30-50wt% monoolefins, 1-10wt% diolefins, 20-30wt% alkanes, 9-20wt% cycloalkanes and 20-40wt% aromatics.

[0086] The method for producing gasoline, diesel and kerosene provided by the present application, in step S1, after the indirect liquefied oil is subjected to the first atmospheric distillation separation and the first vacuum distillation separation, the main component in the obtained fraction is normal alkanes. Through hydrocracking reaction and isomerization reaction (mainly hydrocracking reaction, and also accompanied by hydroisomerization reaction), a first product is obtained, and the first product is subjected to the second atmospheric distillation separation and the second atmospheric pressure and vacuum separation, and the main component in the obtained fraction is isoparaffins. The indirect liquefied oil is subjected to hydrocracking reaction and hydroisomerization reaction, so that the normal alkanes are cracked and converted into isoparaffins, and then the gasoline fraction A, diesel fraction A, the first fraction and diesel fraction B are obtained by the second atmospheric distillation separation and the second atmospheric pressure and vacuum separation to improve the standards of the obtained gasoline, diesel and kerosene.

[0087] In step S2, the MTP by-product mixed aromatics are subjected to aromatization reaction or isomerization reaction (mainly aromatization reaction occurs, accompanied by isomerization reaction of some alkanes), so that most of the olefins in the MTP by-product mixed aromatics are converted into aromatics, and some alkanes are subjected to hydrogenation isomerization reaction to be converted into isoalkanes, and then separated by the first mixed aromatics distillation to obtain gasoline fraction B and diesel fraction C, so as to improve the standards of the obtained gasoline and diesel.

[0088] Since kerosene requires not only a low olefin content but also a requirement for the aromatic content (8 to 25 vol%), in order to make the obtained kerosene meet the requirements, in step S2, the MTP by-product mixed aromatics are subjected to a hydrorefining reaction to convert the olefins and most of the aromatics in the MTP by-product mixed aromatics into alkanes and cycloalkanes (after hydrorefining, the products mainly include normal alkanes, isoalkanes and cycloalkanes), and then separated through a second mixed aromatics distillation to obtain a gasoline fraction C and a kerosene fraction, so as to improve the standard of the obtained kerosene and further improve the standard of the obtained gasoline.

[0089] The diesel fractions obtained by reacting and separating the indirect liquefied oil and the MTP by-product mixed aromatics are blended in a diesel blending kettle, thereby achieving the production of qualified diesel; the gasoline fractions are blended in a gasoline blending kettle, thereby achieving the production of qualified gasoline; the kerosene fraction and the first fraction are blended in a kerosene blending kettle, thereby achieving the production of qualified kerosene. The kerosene obtained in this application has a high standard and can be applied to aviation kerosene (aviation fuel used by aircraft engines).

[0090] In summary, the method for producing gasoline, diesel and kerosene provided in the present application jointly processes the oil products produced by the two processing units of indirect liquefied oil and MTP by-product mixed aromatics, with complementary indicators and improved product quality, thereby being able to produce gasoline, diesel and kerosene that meet national standards with high economic benefits.

[0091] In some embodiments, the diesel fraction B obtained from the first side line outlet of the second vacuum tower can also be directly produced, the diesel fraction C obtained from the bottom outlet of the first mixed aromatic tower can also be directly produced, the gasoline fraction C obtained from the top outlet of the second mixed aromatic tower can also be directly produced, and the kerosene fraction obtained from the bottom outlet of the second mixed aromatic tower can also be directly produced.

[0092] In some embodiments, the first valve provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle (300) is closed, the second valve provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle (100) is opened, and the third valve provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle (100) is opened; the fourth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the aromatization and isomerization reactor (6) is opened, and the fifth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the hydrofining reactor (8) is closed to produce gasoline and diesel; the steps include:

[0093] Step A1, transporting the indirect liquefied oil from the indirect liquefied oil supply tank to the first atmospheric distillation tower (1) for first atmospheric distillation separation, and obtaining a ≥C18 hydrocarbon mixture from the bottom outlet of the first atmospheric distillation tower; transporting the ≥C18 hydrocarbon mixture to the first vacuum distillation tower (2) for first vacuum distillation separation, and obtaining a ≥C40 hydrocarbon mixture from the bottom outlet of the first vacuum distillation tower; transporting the ≥C40 hydrocarbon mixture to the hydrocracking and isomerization reactor (3) for hydrocracking reaction and isomerization reaction to obtain a first product; transporting the first product to the second atmospheric distillation tower (4) for second atmospheric distillation separation, and obtaining a ≥C18 hydrocarbon mixture from the top outlet of the second atmospheric distillation tower. to gasoline fraction A, obtain a first fraction from the second atmospheric first side line outlet, obtain a second fraction from the second atmospheric second side line outlet, and obtain a ≥C16 hydrocarbon mixture from the second atmospheric bottom outlet; the first fraction and the second fraction are mixed to obtain a diesel fraction A; the gasoline fraction A is a C5-C10 hydrocarbon mixture, the diesel fraction A is a C10-C16 hydrocarbon mixture, and the second atmospheric bottom fraction is a ≥C16 hydrocarbon mixture; the ≥C16 hydrocarbon mixture is transported to a second vacuum distillation tower (5) for second vacuum distillation separation, and a diesel fraction B is obtained from the second vacuum first side line outlet, and the diesel fraction B is a C16-C21 hydrocarbon mixture;

[0094] Step A2, subjecting the MTP by-product mixed aromatics to aromatization and isomerization to obtain a second product; subjecting the second product to a first mixed aromatic distillation separation to obtain a gasoline fraction B and a diesel fraction C; the gasoline fraction B is a C5-C12 hydrocarbon mixture, and the diesel fraction C is a C12 hydrocarbon mixture;

[0095] Step A3, mixing diesel fraction A, diesel fraction B and diesel fraction C to obtain diesel; mixing gasoline fraction A and gasoline fraction B to obtain gasoline.

[0096] In other embodiments, the first valve provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle (300) is opened, the second valve provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle (100) is closed, and the third valve provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle (100) is closed; the fourth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the aromatization and isomerization reactor (6) is closed, and the fifth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the hydrotreating reactor (8) is opened to produce gasoline and kerosene; the steps include:

[0097] Step B1, subjecting the indirect liquefied oil to a first atmospheric distillation separation to obtain a ≥C18 hydrocarbon mixture; subjecting the ≥C18 hydrocarbon mixture to a first vacuum distillation separation to obtain a ≥C40 hydrocarbon mixture; subjecting the ≥C40 hydrocarbon mixture to a hydrocracking reaction and an isomerization reaction to obtain a first product; subjecting the first product to a second atmospheric distillation separation to obtain a gasoline fraction A, a sideline fraction and a second atmospheric tower bottom fraction, wherein the sideline fraction includes a first fraction (the fraction discharged from the second atmospheric first sideline outlet is the first fraction); the gasoline fraction A is a C5-C10 hydrocarbon mixture, the first fraction is a C10-C14 hydrocarbon mixture, and the second atmospheric tower bottom fraction is a ≥C16 hydrocarbon mixture; subjecting the ≥C16 hydrocarbon mixture to a second vacuum distillation separation to obtain a diesel fraction B, wherein the diesel fraction B is a C16-C21 hydrocarbon mixture;

[0098] Step B2, subjecting the MTP by-product mixed aromatics to a hydrorefining reaction to obtain a third product; subjecting the third product to a second mixed aromatics distillation separation to obtain a gasoline fraction C and a kerosene fraction; the gasoline fraction C is a C5-C8 hydrocarbon mixture, and the kerosene fraction is a ≥C8 hydrocarbon mixture;

[0099] Step B3, mixing the kerosene fraction and the first fraction to obtain kerosene; mixing the gasoline fraction A and the gasoline fraction C to obtain gasoline.

[0100] In the present invention, "C5-C10 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 5-10", "C10-C14 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 10-14", "C14-C18 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 14-18", and "C18-C21 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 18-21". "C21-C25 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 21-25", "C25-C40 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 25-40", "C14-C16 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 14-16", and "C10-C16 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with carbon numbers of 10-16". "C16-C21 hydrocarbon mixture" refers to "a hydrocarbon mixture with a content of ≥80wt% of hydrocarbons with a carbon number of 16-21", "C5-C12 hydrocarbon mixture" refers to "a hydrocarbon mixture with a content of ≥80wt% of hydrocarbons with a carbon number of 5-12", "C5-C8 hydrocarbon mixture" refers to "a hydrocarbon mixture with a content of ≥80wt% of hydrocarbons with a carbon number of 5-8", and "≥C40 hydrocarbon mixture" refers to "a hydrocarbon mixture with a content of ≥80wt% of hydrocarbons with a carbon number of 40 or more". "≥C12 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with a carbon number of 12 or more", "≥C8 hydrocarbon mixture" refers to "a hydrocarbon mixture containing ≥80wt% of hydrocarbons with a carbon number of 8 or more".

[0101] The present invention does not limit the specific source of the indirect liquefied oil, which can be purchased or prepared by itself. When prepared by itself, the following steps are included: the oil (wax) synthesized by the Fischer-Tropsch synthesis unit is subjected to a hydrorefining reaction to obtain the indirect liquefied oil. MTP by-product mixed aromatics refer to a mixture of mixed aromatics produced by different catalyst cycles of the MTP unit.

[0102] In some embodiments, the temperature of the first atmospheric distillation separation is 250-500° C., and the pressure of the first atmospheric distillation separation is 0.05-2.0 MPa, so as to further purify the indirect liquefied oil and further obtain various oil fractions with high purity.

[0103] Typically but not limitatively, the temperature of the first atmospheric distillation separation is 250°C, 300°C, 350°C, 4000°C, 450°C, 500°C or a range consisting of any two values; the pressure of the first atmospheric distillation separation is 0.05 MPa, 0.1 MPa, 0.5 MPa, 1.0 MPa, 1.5 MPa, 2.0 MPa or a range consisting of any two values.

[0104] In some embodiments, the temperature of the first vacuum distillation separation is 200-400° C., and the pressure of the first vacuum distillation separation is 0-0.1 MPa, so as to further purify the indirect liquefied oil and further obtain various oil fractions with high purity.

[0105] Typically but not limitatively, the temperature of the first vacuum distillation separation is 200°C, 250°C, 300°C, 350°C, 400°C or a range consisting of any two values; the pressure of the first vacuum distillation separation is 0 MPa, 0.02 MPa, 0.04 MPa, 0.06 MPa, 0.08 MPa, 0.10 MPa or a range consisting of any two values.

[0106] In some embodiments, the catalyst for the hydrocracking reaction and the isomerization reaction includes an active component and a carrier, preferably the active component includes Ni and / or W, and the carrier includes alumina and / or a molecular sieve; further preferably, the active component (in terms of NiO and / or WO3) accounts for 4%-30% of the total weight of the catalyst, and further preferably the molecular sieve includes any one or more of Y-type molecular sieve, ZSM-11 molecular sieve, ZSM-35 molecular sieve, and ZSM-48 molecular sieve; the alumina may also include silicon-containing alumina. The above catalyst for the hydrocracking reaction and the isomerization reaction is used to further increase the rate of the hydrocracking reaction and the isomerization reaction.

[0107] In some embodiments, the conditions for the hydrocracking reaction and the isomerization reaction include: a temperature of 280 to 450°C, a pressure of 6 to 13 MPa, and a volume space velocity of 1 to 3.5 h -l , the volume ratio of hydrogen to oil is 400-800:1 to further improve the properties of the oil.

[0108] Typically but not limiting, the temperature of the hydrocracking reaction and the isomerization reaction is 280°C, 300°C, 350°C, 400°C, 450°C or a range consisting of any two values; the pressure of the hydrocracking reaction and the isomerization reaction is 6MPa, 8MPa, 10MPa, 12MPa, 13MPa or a range consisting of any two values; the volume space velocity of the hydrocracking reaction and the isomerization reaction is 1h -l , 1.5h -l , 2h -l , 2.5h-l , 3h -l , 3.5h -l Or a range value consisting of any two numerical values; the hydrogen-oil volume for hydrocracking reaction and isomerization reaction is, for example, 400:1, 500:1, 600:1, 700:1, 800:1 or a range value consisting of any two numerical values.

[0109] In some embodiments, the temperature of the second atmospheric distillation separation is 250-400° C., and the pressure of the second atmospheric distillation separation is 0.1-1.0 MPa, so as to further obtain high-purity gasoline fraction A, diesel fraction A and the first fraction.

[0110] Typically but not limitatively, the temperature of the second atmospheric distillation separation is 250°C, 300°C, 350°C, 400°C or a range consisting of any two values; the pressure of the second atmospheric distillation separation is 0.1 MPa, 0.2 MPa, 0.4 MPa, 0.6 MPa, 0.8 MPa, 1.0 MPa or a range consisting of any two values.

[0111] In some embodiments, the temperature of the second vacuum distillation separation is 200-350° C., and the pressure of the second vacuum distillation separation is 0-0.1 MPa, so as to further obtain a diesel fraction B with high purity.

[0112] Typically but not limitatively, the temperature of the second vacuum distillation separation is 200°C, 250°C, 300°C, 350°C or a range consisting of any two values; the pressure of the second vacuum distillation separation is 0 MPa, 0.02 MPa, 0.04 MPa, 0.06 MPa, 0.10 MPa or a range consisting of any two values.

[0113] In some embodiments, in step S2, the conditions for aromatization reaction and isomerization reaction are: temperature of 260-400°C and pressure of 0.8-1.1 MPa; so as to further convert most of the olefins in the MTP by-product mixed aromatics into aromatics or alkanes, and further make the obtained diesel meet the requirements.

[0114] Typically but not limiting, the temperature of the aromatization reaction and the isomerization reaction is 260°C, 300°C, 350°C, 400°C or a range consisting of any two values; the pressure of the aromatization reaction and the isomerization reaction is 0.8 MPa, 0.9 MPa, 1.0 MPa, 1.1 MPa or a range consisting of any two values.

[0115] In some embodiments, the catalyst for aromatization reaction and isomerization reaction comprises an active component and a carrier, wherein the active component is ZSM-5 molecular sieve and the carrier is alumina; further preferably, the active component accounts for 65%-80% of the total weight of the catalyst, and further preferably, the specific surface area of ​​the catalyst for aromatization reaction and isomerization reaction is 250-300m 2 / g.

[0116] In some embodiments, the temperature of the first mixed aromatics distillation separation is 250-300° C., and the pressure of the first mixed aromatics distillation separation is 0.1-1.0 MPa, so as to further obtain a gasoline fraction B and a diesel fraction C with high purity.

[0117] Typically but not limitatively, the temperature of the first mixed aromatic distillation separation is 250°C, 260°C, 270°C, 280°C, 290°C, 300°C or a range consisting of any two values; the pressure of the first mixed aromatic distillation separation is 0.1 MPa, 0.2 MPa, 0.4 MPa, 0.6 MPa, 0.8 MPa, 1.0 MPa or a range consisting of any two values.

[0118] In some embodiments, the hydrotreating catalyst comprises a hydrogenation active metal and a carrier, the hydrogenation active metal comprises Mo and / or Ni, and the carrier comprises alumina and / or silica. It is further preferred that the hydrogenation active metal (in terms of MoO3 and / or NiO) accounts for 3%-30% of the total weight of the catalyst.

[0119] In some embodiments, in step S2, the conditions for the hydrofining reaction are: temperature of 300-400°C, pressure of 4.5-9.5 MPa, and volume space velocity of 1-4 h -1 , the volume ratio of hydrogen to oil is 300-700:1; to further improve the conversion rate of the hydrorefining reaction, the yield of alkanes and cycloalkanes, and to further improve the standard of the obtained kerosene.

[0120] Typically but not limiting, the temperature of the hydrofining reaction is 300°C, 320°C, 340°C, 360°C, 380°C, 400°C or a range consisting of any two values; the pressure of the hydrofining reaction is 4.5MPa, 5.0MPa, 6.0MPa, 7.0MPa, 8.0MPa, 9.0MPa, 9.5MPa or a range consisting of any two values; the volume space velocity of the hydrofining reaction is 1h -1 , 2h -1 , 3h -1 , 4h -1 Or a range value consisting of any two numerical values; the hydrogen oil volume of the hydrotreating reaction is, for example, 300:1, 400:1, 500:1, 600:1, 700:1 or a range value consisting of any two numerical values.

[0121] In some embodiments, the temperature of the second mixed aromatics distillation separation is 120-200° C., and the pressure of the second mixed aromatics distillation separation is 0.1-1.0 MPa, so as to further obtain a high-purity gasoline fraction C and a kerosene fraction.

[0122] Typically but not limitatively, the temperature of the second mixed aromatic distillation separation is 120°C, 150°C, 180°C, 200°C or a range consisting of any two values; the pressure of the second mixed aromatic distillation separation is 0.1 MPa, 0.2 MPa, 0.4 MPa, 0.6 MPa, 0.8 MPa, 1.0 MPa or a range consisting of any two values.

[0123] In some embodiments, in step S3, the volume ratio of diesel fraction A, diesel fraction B and diesel fraction C is 1:0.01-1:0.6-1, so as to further improve the quality of diesel, thereby further producing diesel that meets national standards.

[0124] Typically but not limiting, the volumes of diesel fraction A, diesel fraction B and diesel fraction C are 1:0.01:1, 1:0.1:1, 1:0.5:1, 1:0.8:0.6, 1:0.8:0.8, 1:1:1 or a range consisting of any two values.

[0125] In some embodiments, the volume ratio of gasoline fraction A to gasoline intermediate is 1:1-2, so as to further improve the quality of gasoline, thereby further producing gasoline that meets national standards.

[0126] Typically but not limiting, the volume ratio of gasoline fraction A to gasoline intermediate is, for example, 1:1, 1:1.2, 1:1.4, 1:1.6, 1:1.8, 1:2 or a range consisting of any two of these values.

[0127] In some embodiments, the volume ratio of the first fraction to the kerosene fraction is 1:1-3; so as to further improve the quality of the kerosene, thereby further producing kerosene that meets national standards.

[0128] Typically but not limiting, the ratio of the first fraction to the kerosene fraction is 1:1, 1:1.5, 1:2, 1:2.5, 1:3 or a range consisting of any two of these values.

[0129] In some embodiments, the kerosene further includes additives to improve the quality of the kerosene.

[0130] In the present application, the optional range of additive types is relatively wide. For the present application, in order to improve the conductivity of kerosene and reduce safety risks, the additive is preferably an antistatic agent, and the antistatic agent is further preferably T1502 and / or Stadis450.

[0131] In some embodiments, the amount of the additive is 1-3 mg / L, that is, relative to 1 L of kerosene, the amount of the additive is 1-3 mg.

[0132] Typically, but not limiting, the amount of the additive used is 1 mg / L, 1.5 mg / L, 2 mg / L, 2.5 mg / L, 3 mg / L or a range consisting of any two values.

[0133] The beneficial effects of the present application will be further illustrated below in conjunction with embodiments.

[0134] In the following examples, the properties of the indirect liquefied oil are shown in Table 1, and the properties of the MTP by-product mixed aromatics are shown in Table 2.

[0135] Table 1

[0136] project Indirect liquefied oil Normal alkanes / wt% 85 Isoparaffin / wt% 14 Aromatics / wt% ＜1 Cycloalkanes / wt% ＜1 <![CDATA[Density (20 °C) / (g / cm 3 )]]> 790

[0137] Table 2

[0138]

[0139]

[0140] Example 1

[0141] This embodiment provides a system for producing gasoline, diesel and kerosene, such as Figure 1 As shown, the system includes: 1. a first atmospheric distillation tower; 2. a first vacuum distillation tower; 3. a hydrocracking and isomerization reactor; 4. a second atmospheric distillation tower; 5. a second vacuum distillation tower; 6. an aromatization and isomerization reactor; 7. a first mixed aromatic distillation tower; 8. a hydrofining reactor; 9. a second mixed aromatic distillation tower; 10. an MTP by-product mixed aromatic supply tank; 100. a diesel blending kettle; 200. a gasoline blending kettle; 300. a kerosene blending kettle.

[0142] The inlet of the first atmospheric distillation tower 1 is connected to the outlet of the indirect liquefied oil supply storage tank, and the indirect liquefied oil supply storage tank is used to store the indirect liquefied oil. The first atmospheric distillation tower 1 has a first atmospheric tower top outlet, a first atmospheric first side line outlet, a first atmospheric second side line outlet and a first atmospheric tower bottom outlet. The first atmospheric first side line outlet is higher than the first atmospheric second side line outlet. The first atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower 2.

[0143] The first vacuum distillation tower 2 has a first vacuum first side line outlet, a first vacuum second side line outlet, a first vacuum third side line outlet and a first vacuum bottom outlet, the first vacuum first side line outlet is higher than the first vacuum second side line outlet, the first vacuum second side line outlet is higher than the first vacuum third side line outlet, and the first vacuum bottom outlet is connected to the inlet of the hydrocracking and isomerization reactor 3.

[0144] The outlet of the hydrocracking and isomerization reactor 3 is connected to the inlet of the second atmospheric distillation tower 4. The second atmospheric distillation tower 4 has a second atmospheric tower top outlet, a second atmospheric pressure first side line outlet, a second atmospheric pressure second side line outlet and a second atmospheric pressure tower bottom outlet. The second atmospheric pressure first side line outlet is higher than the second atmospheric pressure second side line outlet. The second atmospheric pressure tower bottom outlet is connected to the inlet of the first vacuum distillation tower 5.

[0145] The second vacuum distillation tower 5 has a second vacuum first sideline outlet, a second vacuum second sideline outlet, a second vacuum third sideline outlet and a second vacuum tower bottom outlet.

[0146] The inlet of the aromatization and isomerization reactor 6 is connected to the outlet of the MTP by-product mixed aromatics supply storage tank 10, and the MTP by-product mixed aromatics supply storage tank 10 is used to store the MTP by-product mixed aromatics. The outlet of the aromatization and isomerization reactor 6 is connected to the inlet of the first mixed aromatics distillation tower 7, and the first mixed aromatics distillation tower 7 has a first mixed aromatics tower top outlet and a first mixed aromatics tower bottom outlet.

[0147] The inlet of the hydrotreating reactor 8 is connected to the outlet of the MTP by-product mixed aromatics supply tank 10, and the outlet of the hydrotreating reactor 8 is connected to the inlet of the second mixed aromatics distillation tower 9. The second mixed aromatics distillation tower 9 has a second mixed aromatics tower top outlet and a second mixed aromatics tower bottom outlet.

[0148] The diesel blending kettle 100 has a first diesel inlet, a second diesel inlet, a third diesel inlet and a fourth diesel inlet. The second normal pressure first side line outlet is connected to the first diesel inlet of the diesel blending kettle 100, the second normal pressure second side line outlet is connected to the second diesel inlet of the diesel blending kettle 100, the second reduced pressure first side line outlet is connected to the third diesel inlet of the diesel blending kettle 100, and the first mixed aroma tower bottom outlet is connected to the fourth diesel inlet of the diesel blending kettle 100.

[0149] The gasoline blending kettle 200 has a first gasoline inlet, a second gasoline inlet and a third gasoline inlet. The second atmospheric tower top outlet is connected to the first gasoline inlet of the gasoline blending kettle 200, the first mixed aroma tower top outlet is connected to the second gasoline inlet of the gasoline blending kettle 200; the second mixed aroma tower top outlet is connected to the third gasoline inlet of the gasoline blending kettle 200.

[0150] The kerosene blending kettle 300 has a first kerosene inlet, a second kerosene inlet and an additive inlet, the second normal pressure first side line outlet is connected to the first kerosene inlet of the kerosene blending kettle 300, and the second mixed aroma tower bottom outlet is connected to the second kerosene inlet of the kerosene blending kettle 300. The additive inlet is used to provide additives to the kerosene blending kettle 300.

[0151] A first valve is provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle 300, a second valve is provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle 100, and a third valve is provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle 100;

[0152] A fourth valve is provided on the pipeline connecting the MTP by-product mixed aromatics supply tank 10 and the aromatization and isomerization reactor 6 ; a fifth valve is provided on the pipeline connecting the MTP by-product mixed aromatics supply tank 10 and the hydrotreating reactor 8 .

[0153] The system also includes a plurality of flowmeters for controlling the addition amount of each blending component in the preparation of kerosene, diesel or gasoline, so as to produce oil products with stable quality. A first flowmeter is provided on the pipeline connecting the second normal pressure first side line outlet with the first diesel inlet of the diesel blending kettle 100, a second flowmeter is provided on the pipeline connecting the second normal pressure second side line outlet with the second diesel inlet of the diesel blending kettle 100, a third flowmeter is provided on the pipeline connecting the second reduced pressure first side line outlet with the third diesel inlet of the diesel blending kettle 100; a fourth flowmeter is provided on the pipeline connecting the first mixed aromatic tower bottom outlet with the fourth diesel inlet of the diesel blending kettle 100.

[0154] A fifth flowmeter is provided on the pipeline connecting the top outlet of the second atmospheric tower with the first gasoline inlet of the gasoline blending kettle 200, a sixth flowmeter is provided on the pipeline connecting the top outlet of the first mixed aromatization tower with the second gasoline inlet of the gasoline blending kettle 200, and a seventh flowmeter is provided on the pipeline connecting the top outlet of the second mixed aromatization tower with the third gasoline inlet of the gasoline blending kettle 200.

[0155] An eighth flow meter is provided on the pipeline connecting the second normal pressure first side line outlet with the first kerosene inlet of the kerosene blending kettle 300, and a ninth flow meter is provided on the pipeline connecting the second mixed aromatic tower bottom outlet with the second kerosene inlet of the kerosene blending kettle 300.

[0156] Example 2

[0157] The present embodiment provides a method for producing gasoline and diesel, in which the system in Example 1 is used, the first valve provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle 300 is closed; the second valve provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle 100 is opened; the third valve provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle 100 is opened; the fourth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank 10 and the aromatization and isomerization reactor 6 is opened; the fifth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank 10 and the hydrofining reactor 8 is closed;

[0158] The method for producing gasoline and diesel specifically comprises the following steps:

[0159] (1) The indirect liquefied oil in the indirect liquefied oil supply tank is transported to the first atmospheric distillation tower 1 for first atmospheric distillation separation (operating conditions include: temperature of 340° C., pressure of 0.15 MPa), to obtain a C5-C10 hydrocarbon mixture (discharged from the first atmospheric tower top outlet), a C10-C14 hydrocarbon mixture (discharged from the first atmospheric first side line outlet), a C14-C18 hydrocarbon mixture (discharged from the first atmospheric second side line outlet), and a C18 hydrocarbon mixture (discharged from the first atmospheric tower bottom outlet).

[0160] The ≥C18 hydrocarbon mixture (discharged from the bottom outlet of the first atmospheric pressure tower) is transported to the first vacuum distillation tower 2 for the first vacuum distillation (operating conditions include: temperature of 310°C, pressure of 0.01MPa) to obtain a C18-C21 hydrocarbon mixture (discharged from the first vacuum first side line outlet), a C21-C25 hydrocarbon mixture (discharged from the first vacuum second side line outlet), a C25-C40 hydrocarbon mixture (discharged from the first vacuum third side line outlet) and a ≥C40 hydrocarbon mixture (discharged from the bottom outlet of the first vacuum tower).

[0161] The ≥C40 hydrocarbon mixture (discharged from the bottom outlet of the first vacuum tower) is transported to the hydrocracking and isomerization reactor 3 for the first reaction. The operating conditions are: temperature 360°C, pressure 8MPa, volume space velocity 2h -l The volume ratio of hydrogen to oil is 500:1. The catalyst used in the hydrocracking reaction and the isomerization reaction is Ni / Al2O3, and the active component (calculated as NiO) accounts for 10% of the total weight of the catalyst.

[0162] The obtained first product is transported to the second atmospheric distillation tower 4 for second atmospheric distillation separation (operating conditions include: temperature of 310°C, pressure of 0.1MPa) to obtain gasoline fraction A (discharged from the second atmospheric tower top outlet), gasoline fraction A is a C5-C10 hydrocarbon mixture, a C10-C14 hydrocarbon mixture (discharged from the second atmospheric first side line outlet), a C14-C16 hydrocarbon mixture (discharged from the second atmospheric second side line outlet) and a ≥C16 hydrocarbon mixture (discharged from the second atmospheric tower bottom outlet), wherein the first fraction is discharged from the second atmospheric first side line outlet, the second fraction is discharged from the second atmospheric second side line outlet, the first fraction and the second fraction are mixed to form diesel fraction A, and diesel fraction A is a C10-C16 hydrocarbon mixture.

[0163] The fraction at the bottom outlet of the second atmospheric tower is transported to the second vacuum distillation tower 5 for second vacuum distillation separation (operating conditions include: temperature of 300° C., pressure of 0.03 MPa) to obtain a diesel fraction B (discharged from the second vacuum first side line outlet), the diesel fraction B is a C16-C21 hydrocarbon mixture, a C21-C25 hydrocarbon mixture (discharged from the second vacuum second side line outlet), a C25-C40 hydrocarbon mixture (discharged from the second vacuum third side line outlet), and a ≥C40 hydrocarbon mixture (discharged from the second vacuum tower bottom outlet);

[0164] (2) The MTP by-product mixed aromatics in the MTP by-product mixed aromatics supply tank 10 are transported to the aromatization and isomerization reactor 6 for aromatization and isomerization reaction (operating conditions include: 0.9 MPa, 350° C.), and the catalyst used in the aromatization and isomerization reaction is ZSM-5 / Al2O3, where ZSM-5 accounts for 70% of the total weight of the catalyst and the specific surface area of ​​the catalyst is 250 m 2 / g; the obtained second product is transported to the first mixed aromatic distillation tower 7, and the first mixed aromatic distillation separation is carried out (the operating conditions include: temperature is 286°C, pressure is 0.1MPa), and a gasoline fraction B (discharged from the top outlet of the first mixed aromatic tower) and a diesel fraction C (discharged from the bottom outlet of the first mixed aromatic tower) are obtained, the gasoline fraction B is a C5-C12 hydrocarbon mixture, and the diesel fraction C is a ≥C12 hydrocarbon mixture;

[0165] (3) The diesel fraction A obtained in the second atmospheric distillation tower 4, the diesel fraction B obtained in the second vacuum distillation tower 5, and the diesel fraction C obtained in the first mixed aromatic distillation tower 7 are respectively transported to the diesel blending kettle 100, and blended in the diesel blending kettle 100 to obtain diesel; wherein the volume ratio of the diesel fraction A, the diesel fraction B, and the diesel fraction C is 1:0.2:0.8;

[0166] (4) The gasoline fraction A obtained in the second atmospheric distillation tower 4 and the gasoline fraction B obtained in the first mixed aromatic distillation tower 7 are transported to the gasoline blending kettle 200 and blended in the gasoline blending kettle 200 to obtain gasoline. The volume ratio of the gasoline fraction A to the gasoline fraction B is 1:1.

[0167] Example 3

[0168] The present embodiment provides a method for producing gasoline and kerosene, in which the system in Example 1 is used, the first valve provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle 300 is opened; the second valve provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle 100 is closed; the third valve provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle 100 is closed; the fourth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank 10 and the aromatization and isomerization reactor 6 is closed; the fifth valve provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank 10 and the hydrofining reactor 8 is opened;

[0169] The method for producing gasoline and kerosene specifically comprises the following steps:

[0170] (1) The indirect liquefied oil in the indirect liquefied oil supply tank is transported to the first atmospheric distillation tower 1 for first atmospheric distillation separation (operating conditions include: temperature of 340° C., pressure of 0.15 MPa), to obtain a C5-C10 hydrocarbon mixture (discharged from the first atmospheric tower top outlet), a C10-C14 hydrocarbon mixture (discharged from the first atmospheric first side line outlet), a C14-C18 hydrocarbon mixture (discharged from the first atmospheric second side line outlet), and a C18 hydrocarbon mixture (discharged from the first atmospheric tower bottom outlet).

[0171] The ≥C18 hydrocarbon mixture (discharged from the bottom outlet of the first atmospheric pressure tower) is transported to the first vacuum distillation tower 2 for first vacuum distillation separation (operating conditions include: temperature of 310°C, pressure of 0.01MPa) to obtain a C18-C21 hydrocarbon mixture (discharged from the first vacuum first side line outlet), a C21-C25 hydrocarbon mixture (discharged from the first vacuum second side line outlet), a C25-C40 hydrocarbon mixture (discharged from the first vacuum third side line outlet) and a ≥C40 hydrocarbon mixture (discharged from the bottom outlet of the first vacuum tower).

[0172] The ≥C40 hydrocarbon mixture (discharged from the bottom outlet of the first vacuum tower) is sent to the hydrocracking and isomerization reactor 3 for the first reaction. The operating conditions are: temperature 360°C, pressure 8MPa, volume space velocity 2h -l The volume ratio of hydrogen to oil is 500:1. The catalyst used in the hydrocracking and isomerization reactions is Ni / Al2O3, and the active component (calculated as NiO) accounts for 10% of the total weight of the catalyst.

[0173] The obtained first product is transported to the second atmospheric distillation tower 4 for second atmospheric distillation separation (operating conditions include: temperature of 310°C, pressure of 0.1MPa), to obtain a gasoline fraction A (discharged from the second atmospheric tower top outlet), the gasoline fraction A is a C5-C10 hydrocarbon mixture, a C10-C14 hydrocarbon mixture (discharged from the second atmospheric first side line outlet), a C14-C16 hydrocarbon mixture (discharged from the second atmospheric second side line outlet) and a ≥C16 hydrocarbon mixture (discharged from the second atmospheric tower bottom outlet), wherein the fraction discharged from the second atmospheric first side line outlet is the first fraction The ≥C16 hydrocarbon mixture (discharged from the second atmospheric tower bottom outlet) is transported to the second vacuum distillation tower 5 for second vacuum distillation separation (operating conditions include: temperature of 300°C, pressure of 0.03Mpa) to obtain a diesel fraction B (discharged from the second vacuum first side line outlet), the diesel fraction B is a C16-C21 hydrocarbon mixture, a C21-C25 hydrocarbon mixture (discharged from the second vacuum second side line outlet), a C25-C40 hydrocarbon mixture (discharged from the second vacuum third side line outlet), and a ≥C40 hydrocarbon mixture (discharged from the second vacuum tower bottom outlet);

[0174] (2) The MTP by-product mixed aromatics in the MTP by-product mixed aromatics supply tank 10 are transported to the hydrotreating reactor 8 for hydrotreating reaction (operating conditions include: temperature of 350° C., pressure of 8 MPa, volumetric space velocity of 1 h -1 , the volume ratio of hydrogen to oil is 500:1), the catalyst used in the hydrotreating reaction is Mo / Al2O3, and the hydrogenation active metal (calculated as MoO3) accounts for 10% of the total weight of the catalyst; the obtained product is transported to the second mixed aromatic distillation tower 9, and the second mixed aromatic distillation separation is carried out (the operating conditions include: temperature is 160°C, pressure is 0.1MPa), and a gasoline fraction C (discharged from the top outlet of the second mixed aromatic tower) and a kerosene fraction (discharged from the bottom outlet of the second mixed aromatic tower) are obtained; the gasoline fraction C is a C5-C8 hydrocarbon mixture, and the kerosene fraction is a ≥C8 hydrocarbon mixture.

[0175] (3) The first fraction obtained in the second atmospheric distillation tower 4, the kerosene fraction obtained in the second mixed aromatic distillation tower 9, and the antistatic agent are respectively transported to the kerosene blending kettle 300, and blended in the kerosene blending kettle 300 to obtain kerosene; wherein the volume ratio of the first fraction to the kerosene fraction is 1:2, and the amount of the antistatic agent (T1502) added is 3 mg / L (i.e., the amount of the antistatic agent added is 3 mg per liter of the total amount of kerosene);

[0176] (4) The gasoline fraction A obtained in the second atmospheric distillation tower 4 and the gasoline fraction C obtained in the second mixed aromatic distillation tower 9 are transported to the gasoline blending kettle 200 and blended in the gasoline blending kettle 200 to obtain gasoline. The volume ratio of the gasoline fraction A to the gasoline fraction C is 1:1.

[0177] Example 4

[0178] This embodiment provides a method for producing gasoline, diesel and kerosene, wherein the method uses the system in Embodiment 1 and specifically comprises the following steps:

[0179] (1) The indirect liquefied oil is transported from the indirect liquefied oil supply tank to the first atmospheric distillation tower 1 for first atmospheric distillation separation (operating conditions include: temperature of 340° C., pressure of 0.15 MPa), to obtain a C5-C10 hydrocarbon mixture (discharged from the first atmospheric tower top outlet), a C10-C14 hydrocarbon mixture (discharged from the first atmospheric first side line outlet), a C14-C18 hydrocarbon mixture (discharged from the first atmospheric second side line outlet), and a C18 hydrocarbon mixture (discharged from the first atmospheric tower bottom outlet).

[0180] The ≥C18 hydrocarbon mixture (discharged from the bottom outlet of the first atmospheric pressure tower) is transported to the first vacuum distillation tower 2 for first vacuum distillation separation (operating conditions include: temperature of 310°C, pressure of 0.01MPa) to obtain a C18-C21 hydrocarbon mixture (discharged from the first vacuum first side line outlet), a C21-C25 hydrocarbon mixture (discharged from the first vacuum second side line outlet), a C25-C40 hydrocarbon mixture (discharged from the first vacuum third side line outlet) and a ≥C40 hydrocarbon mixture (discharged from the bottom outlet of the first vacuum tower).

[0181] The ≥C40 hydrocarbon mixture (discharged from the bottom outlet of the first vacuum tower) is transported to the hydrocracking and isomerization reactor 3 for the first reaction. The operating conditions are: temperature 360°C, pressure 8MPa, volume space velocity 2h -l The volume ratio of hydrogen to oil is 500: 1. The catalyst used in the hydrocracking and isomerization reactions is Ni / Al2O3, and the active component (calculated as NiO) accounts for 10% of the total weight of the catalyst.

[0182] The obtained first product is transported to the second atmospheric distillation tower 4 for second atmospheric distillation separation (operating conditions include: temperature of 310° C., pressure of 0.1 MPa), to obtain a gasoline fraction A (discharged from the second atmospheric tower top outlet), the gasoline fraction A is a C5-C10 hydrocarbon mixture, a C10-C14 hydrocarbon mixture (discharged from the second atmospheric first side line outlet), a C14-C16 hydrocarbon mixture (discharged from the second atmospheric second side line outlet) and a ≥C16 hydrocarbon mixture (discharged from the second atmospheric tower bottom outlet), wherein the fraction discharged from the second atmospheric first side line outlet is the first fraction, and the first fraction discharged from the second atmospheric first side line outlet and the second fraction discharged from the second atmospheric second side line outlet are mixed to form a diesel fraction A;

[0183] The ≥C16 hydrocarbon mixture (discharged from the second atmospheric pressure tower bottom outlet) is transported to the second vacuum distillation tower 5 for second vacuum distillation separation (operating conditions include: temperature of 300°C, pressure of 0.03Mpa) to obtain a diesel fraction B (discharged from the second vacuum first side line outlet). The diesel fraction B is a C16-C21 hydrocarbon mixture, a C21-C25 hydrocarbon mixture (discharged from the second vacuum second side line outlet), a C25-C40 hydrocarbon mixture (discharged from the second vacuum third side line outlet), and a ≥C40 hydrocarbon mixture (discharged from the second vacuum tower bottom outlet).

[0184] (2) The MTP by-product mixed aromatics in the MTP by-product mixed aromatics supply tank 10 are transported to the aromatization and isomerization reactor 6 for aromatization and isomerization reaction (operating conditions include 0.9 MPa, 350° C.). The catalyst used in the aromatization and isomerization reaction is ZSM-5 / Al2O3, where ZSM-5 accounts for 70% of the total weight of the catalyst and the specific surface area of ​​the catalyst is 250 m 2 / g; the obtained second product is conveyed to the first mixed aromatic distillation tower 7, and the first mixed aromatic distillation separation is carried out (the operating conditions include: temperature is 286°C, pressure is 0.1MPa), and a gasoline fraction B (discharged from the top outlet of the first mixed aromatic tower) and a diesel fraction C (discharged from the bottom outlet of the first mixed aromatic tower) are obtained; the gasoline fraction B is a C5-C12 hydrocarbon mixture, and the diesel fraction C is a ≥C40 hydrocarbon mixture.

[0185] (3) The MTP by-product mixed aromatics in the MTP by-product mixed aromatics supply tank 10 are transported to the hydrotreating reactor 8 for hydrotreating reaction (operating conditions include: temperature of 350° C., pressure of 8 MPa, volumetric space velocity of 1 h -1 , the volume ratio of hydrogen to oil is 500:1); the catalyst used in the hydrofining reaction is Mo / Al2O3, and the hydrogenation active metal (in terms of MoO3) accounts for 10% of the total weight of the catalyst. The obtained product is transported to the second mixed aromatic distillation tower 9 for the second mixed aromatic distillation (operating conditions include: temperature of 160°C and pressure of 0.1MPa) to obtain a gasoline fraction C (discharged from the top outlet of the second mixed aromatic tower) and a kerosene fraction (discharged from the bottom outlet of the second mixed aromatic tower); the gasoline fraction C is a C5-C8 hydrocarbon mixture, and the kerosene fraction is a ≥C8 hydrocarbon mixture.

[0186] (4) The diesel fraction A obtained in the second atmospheric distillation tower 4, the diesel fraction B obtained in the second vacuum distillation tower 5, and the diesel fraction C obtained in the first mixed aromatic distillation tower 7 are respectively transported to the diesel blending kettle 100, and blended in the diesel blending kettle 100 to obtain diesel; wherein the volume ratio of the diesel fraction A, the diesel fraction B, and the diesel fraction C is 1:0.5:1;

[0187] (5) The first fraction obtained in the second atmospheric distillation tower 4, the kerosene fraction obtained in the second mixed aromatic distillation tower 9, and the antistatic agent are respectively transported to the kerosene blending kettle 300, and blended in the kerosene blending kettle 300 to obtain kerosene; wherein the volume ratio of the first fraction to the kerosene fraction is 1:1, and the amount of the antistatic agent (T1502) added is 3 mg / L (i.e., the amount of the antistatic agent added is 3 mg per liter of the total amount of kerosene);

[0188] (6) The gasoline fraction A and the gasoline intermediate obtained in the second atmospheric distillation tower 4 are respectively transported to the gasoline blending kettle 200, and blended in the gasoline blending kettle 200 to obtain gasoline. The gasoline intermediate includes the gasoline fraction B in the first mixed aromatic distillation tower 7 and the gasoline fraction C obtained in the second mixed aromatic distillation tower 9, and the volume ratio of the gasoline fraction A to the gasoline intermediate is 1:2.

[0189] Comparative Example 1

[0190] The difference from Example 2 is that no aromatization and isomerization reactions are carried out in step (2).

[0191] Comparative Example 2

[0192] The difference from Example 3 is that no hydrotreating reaction is performed in step (2).

[0193] Test Case

[0194] 1. The gasoline prepared in Examples 2-4 and Comparative Examples 1-2 was tested according to the National VI gasoline method. The properties of the oil and the National VI gasoline standard are shown in Table 3.

[0195] Table 3

[0196]

[0197] 2. The diesel produced in Examples 2, 4 and Comparative Example 1 was tested according to the National VI automotive diesel method. The properties of the oil and the National VI diesel standard are shown in Table 4.

[0198] Table 4

[0199]

[0200] 3. The kerosene prepared in Examples 3-4 and Comparative Example 2 was tested according to the No. 3 jet fuel method. The properties of the oil products and the GB6537-2018 standard are shown in Table 5.

[0201] Table 5

[0202]

[0203] It can be seen from the experimental results of Examples 2-4 and Comparative Examples 1-2 that the system and method of the present application are used to jointly process the oil products produced by the two processing units of indirect liquefied oil and MTP by-product mixed aromatics, with complementary indicators and improved product quality. It is possible to prepare gasoline and diesel that meet national standards, or gasoline and kerosene that meet national standards, or gasoline, diesel and kerosene that meet national standards. When the MTP by-product mixed aromatics are not subjected to aromatization and isomerization reactions, or are not subjected to hydrofining reactions, the oil products of the obtained gasoline, kerosene or diesel are poor and do not meet national standards.

[0204] From the above description, it can be seen that the above embodiments of the present invention achieve the following technical effects:

[0205] The system for producing gasoline, diesel and kerosene provided by the present invention adopts a first atmospheric distillation tower and a first vacuum distillation tower to distill and purify the indirect liquefied oil to obtain hydrocarbons ≥C40, adopts a hydrocracking and isomerization reactor to hydrocrack and hydroisomerize the hydrocarbons ≥C40, and then separates them through a second atmospheric tower and a second vacuum distillation tower to obtain a gasoline fraction A, a diesel fraction A, a first fraction and a diesel fraction B;

[0206] The olefins in the MTP by-product mixed aromatics are converted into aromatics or alkanes by aromatization and isomerization reactors, solving the problems of excessive olefins and diolefins, unqualified oxidation stability and colloid content in the MTP by-product mixed aromatics. The mixture is then separated by the first mixed aromatics distillation tower to obtain gasoline fraction B and diesel fraction C.

[0207] A hydrotreating reactor is used to convert olefins and most of the aromatics in the MTP by-product mixed aromatics into alkanes and cycloalkanes, solving the problem of high olefin and aromatic content in the MTP by-product mixed aromatics. The mixture is then separated through a second aromatic distillation tower to obtain gasoline fraction C and kerosene fraction.

[0208] The diesel fractions obtained by reacting and separating the indirect liquefied oil and the MTP by-product mixed aromatics are blended in a diesel blending kettle, thereby achieving the production of qualified diesel; the gasoline fractions are blended in a gasoline blending kettle, thereby achieving the production of qualified gasoline; the kerosene fraction and the first fraction are blended in a kerosene blending kettle, thereby achieving the production of qualified kerosene.

[0209] In summary, the system for producing gasoline, diesel and kerosene provided in the present application jointly processes the oil products produced by the two processing units of indirect liquefied oil and MTP by-product mixed aromatics, with complementary indicators and improved product quality, thereby being able to produce gasoline, diesel and kerosene that meet national standards with high economic benefits.

[0210] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A system for producing gasoline, diesel and kerosene, characterized in that: include: A raw material supply unit, the raw material supply unit comprising an indirect liquefied oil supply storage tank and an MTP by-product mixed aromatics supply storage tank (10); An indirect liquefied oil processing unit, the indirect liquefied oil processing unit comprises a first atmospheric distillation tower (1), a first vacuum distillation tower (2), a hydrocracking and isomerization reactor (3), a second atmospheric distillation tower (4) and a second vacuum distillation tower (5) connected in sequence; wherein: The inlet of the first atmospheric distillation tower (1) is connected to the outlet of the indirect liquefied oil supply storage tank, the first atmospheric distillation tower (1) has a first atmospheric tower bottom outlet, the first atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower (2), the first vacuum distillation tower (2) has a first vacuum tower bottom outlet, the first vacuum tower bottom outlet is connected to the inlet of the hydrocracking and isomerization reactor (3), the outlet of the hydrocracking and isomerization reactor (3) is connected to the inlet of the second atmospheric distillation tower (4), the second atmospheric distillation tower (4) has a second atmospheric tower top outlet, a second atmospheric first side line outlet, a second atmospheric second side line outlet and a second atmospheric tower bottom outlet, the second atmospheric tower bottom outlet is connected to the inlet of the first vacuum distillation tower (5), and the second vacuum distillation tower (5) has a second vacuum first side line outlet; An MTP by-product mixed aromatics processing unit, the MTP by-product mixed aromatics processing unit comprising an aromatization and isomerization reactor (6), a first mixed aromatics distillation tower (7), a hydrofining reactor (8) and a second mixed aromatics distillation tower (9); wherein: The inlet of the aromatization and isomerization reactor (6) is connected to the outlet of the MTP by-product mixed aromatic hydrocarbon supply storage tank (10), and the outlet of the aromatization and isomerization reactor (6) is connected to the inlet of the first mixed aromatic distillation tower (7), and the first mixed aromatic distillation tower (7) has a first mixed aromatic tower top outlet and a first mixed aromatic tower bottom outlet; The inlet of the hydrotreating reactor (8) is connected to the outlet of the MTP by-product mixed aromatic hydrocarbon supply storage tank (10), and the outlet of the hydrotreating reactor (8) is connected to the inlet of the second mixed aromatic distillation tower (9), and the second mixed aromatic distillation tower (9) has a second mixed aromatic tower top outlet and a second mixed aromatic tower bottom outlet; A blending unit, the blending unit comprising a diesel blending kettle (100), a gasoline blending kettle (200) and a kerosene blending kettle (300); The diesel blending kettle (100) has a first diesel inlet, a second diesel inlet, a third diesel inlet and a fourth diesel inlet, the second normal pressure first side line outlet is connected to the first diesel inlet of the diesel blending kettle (100), the second normal pressure second side line outlet is connected to the second diesel inlet of the diesel blending kettle (100), the second reduced pressure first side line outlet is connected to the third diesel inlet of the diesel blending kettle (100), and the first mixed aromatic tower bottom outlet is connected to the fourth diesel inlet of the diesel blending kettle (100); The gasoline blending kettle (200) has a first gasoline inlet, a second gasoline inlet and a third gasoline inlet, the second atmospheric tower top outlet is connected to the first gasoline inlet of the gasoline blending kettle (200), the first mixed aromatic tower top outlet is connected to the second gasoline inlet of the gasoline blending kettle (200); the second mixed aromatic tower top outlet is connected to the third gasoline inlet of the gasoline blending kettle (200); The kerosene blending kettle (300) has a first kerosene inlet and a second kerosene inlet, the second normal pressure first side line outlet is connected to the first kerosene inlet of the kerosene blending kettle (300), and the second mixed aromatic tower bottom outlet is connected to the second kerosene inlet of the kerosene blending kettle (300).

2. The system for producing gasoline, diesel and kerosene according to claim 1, characterized in that: The first atmospheric distillation tower (1) further comprises a first atmospheric tower top outlet, a first atmospheric first side line outlet and a first atmospheric second side line outlet, wherein the first atmospheric first side line outlet is higher than the first atmospheric second side line outlet; And / or, the first vacuum distillation tower (2) further comprises a first vacuum first side line outlet, a first vacuum second side line outlet and a first vacuum third side line outlet; the first vacuum first side line outlet is higher than the first vacuum second side line outlet, and the first vacuum second side line outlet is higher than the first vacuum third side line outlet.

3. The system for producing gasoline, diesel and kerosene according to claim 1, characterized in that: The second atmospheric pressure first side line outlet of the second atmospheric pressure rectification tower (4) is higher than the second atmospheric pressure second side line outlet; And / or, the second vacuum distillation tower (5) further comprises a second vacuum second side line outlet, a second vacuum third side line outlet and a second vacuum tower bottom outlet; the second vacuum first side line outlet is higher than the second vacuum second side line outlet, and the second vacuum second side line outlet is higher than the second vacuum third side line outlet.

4. The system for producing gasoline, diesel and kerosene according to claim 1, characterized in that: A first valve is provided on the pipeline connecting the second normal pressure first side line outlet and the kerosene blending kettle (300); And / or, a second valve is provided on the pipeline connecting the second normal pressure first side line outlet and the diesel blending kettle (100); And / or, a third valve is provided on the pipeline connecting the second normal pressure second side line outlet and the diesel blending kettle (100); and / or, a fourth valve is provided on the pipeline connecting the MTP by-product mixed aromatic hydrocarbon supply storage tank (10) and the aromatization and isomerization reactor (6); And / or, a fifth valve is provided on the pipeline connecting the MTP by-product mixed aromatics supply storage tank (10) and the hydrotreating reactor (8).

5. The system for producing gasoline, diesel and kerosene according to claim 1, characterized in that: The diesel blending kettle (100) has a diesel outlet at the bottom thereof; And / or, the gasoline blending kettle (200) has a gasoline outlet at the bottom thereof; And / or, the bottom of the kerosene blending kettle (300) has a kerosene outlet; And / or, the kerosene blending kettle (300) further comprises an additive inlet, and the additive inlet is used to provide additives to the kerosene blending kettle (300).

6. A method for producing gasoline, diesel and kerosene, characterized in that: The method comprises the following steps: Step S1, subjecting the indirect liquefied oil to a first atmospheric distillation separation to obtain a ≥C18 hydrocarbon mixture; subjecting the ≥C18 hydrocarbon mixture to a first vacuum distillation separation to obtain a ≥C40 hydrocarbon mixture; subjecting the ≥C40 hydrocarbon mixture to a hydrocracking reaction and an isomerization reaction to obtain a first product; subjecting the first product to a second atmospheric distillation separation to obtain a gasoline fraction A, a side fraction and a second atmospheric bottom fraction, wherein the side fraction includes a diesel fraction A and / or a first fraction; the gasoline fraction A is a C5-C10 hydrocarbon mixture, the first fraction is a C10-C14 hydrocarbon mixture, the diesel fraction A is a C10-C16 hydrocarbon mixture, and the second atmospheric bottom fraction is a ≥C16 hydrocarbon mixture; subjecting the ≥C16 hydrocarbon mixture to a second vacuum distillation separation to obtain a diesel fraction B, wherein the diesel fraction B is a C16-C21 hydrocarbon mixture; Step S2, subjecting the MTP by-product mixed aromatics to aromatization and isomerization to obtain a second product; subjecting the second product to a first mixed aromatic distillation separation to obtain a gasoline fraction B and a diesel fraction C; the gasoline fraction B is a C5-C12 hydrocarbon mixture, and the diesel fraction C is a C12 hydrocarbon mixture; The mixed aromatic hydrocarbons produced as a byproduct of MTP are subjected to a hydrotreating reaction to obtain a third product; the third product is subjected to a second mixed aromatic distillation separation to obtain a gasoline fraction C and a kerosene fraction; the gasoline fraction is a C5-C8 hydrocarbon mixture, and the kerosene fraction is a ≥C8 hydrocarbon mixture; Step S3, mixing the diesel fraction A, the diesel fraction B and the diesel fraction C to obtain diesel; mixing the gasoline fraction A and a gasoline intermediate to obtain gasoline; wherein the gasoline intermediate includes the gasoline fraction B and / or the gasoline fraction C; mixing the kerosene fraction and the first fraction to obtain kerosene; The indirect liquefied oil comprises 80-90 wt% normal alkanes, 9-19 wt% isoalkanes, 0.01-1 wt% aromatics and 0.01-1 wt% cycloalkanes; The MTP byproduct mixed aromatic hydrocarbons include 30-50 wt% of monoolefins, 1-10 wt% of diolefins, 20-30 wt% of alkanes, 9-20 wt% of cycloalkanes and 20-40 wt% of aromatic hydrocarbons.

7. The method for producing gasoline, diesel and kerosene according to claim 6, characterized in that: In the step S1, the temperature of the first atmospheric distillation separation is 250-500° C., and the pressure of the first atmospheric distillation separation is 0.05-2.0 MPa; and / or, the temperature of the first vacuum distillation separation is 200-400° C., and the pressure of the first vacuum distillation separation is 0-0.1 MPa; And / or, the conditions of the hydrocracking reaction and the isomerization reaction include: temperature of 280-450°C, pressure of 6-13 MPa, volume space velocity of 1-3.5 h -l , the volume ratio of hydrogen to oil is 400-800:1; and / or, the temperature of the second atmospheric distillation separation is 250-400° C., and the pressure of the second atmospheric distillation separation is 0.1-1.0 MPa; And / or, the temperature of the second vacuum distillation separation is 200-350° C., and the pressure of the second vacuum distillation separation is 0-0.1 MPa.

8. The method for producing gasoline, diesel and kerosene according to claim 6, characterized in that: In step S2, the conditions of the aromatization reaction and the isomerization reaction are: temperature of 260-400° C. and pressure of 0.8-1.1 MPa; And / or, the temperature of the first mixed aromatic distillation separation is 250-300° C., and the pressure of the first mixed aromatic distillation separation is 0.1-1.0 MPa.

9. The method for producing gasoline, diesel and kerosene according to claim 6, characterized in that: In step S2, the conditions of the hydrotreating reaction are: temperature of 300-400°C, pressure of 4.5-9.5 MPa, volume space velocity of 1-4 h -1 , the volume ratio of hydrogen to oil is 300-700:1; And / or, the temperature of the second mixed aromatic distillation separation is 120-200° C., and the pressure of the second mixed aromatic distillation separation is 0.1-1.0 MPa.

10. The method for producing gasoline, diesel and kerosene according to claim 6, characterized in that: In the step S3, the volume ratio of the diesel fraction A, the diesel fraction B and the diesel fraction C is 1:0.01-1:0.6-1; and / or, the volume ratio of the gasoline fraction A to the gasoline intermediate is 1:1-2; and / or, the volume ratio of the first fraction to the kerosene fraction is 1:1-3; And / or, in step S3, the kerosene further includes an additive; Preferably, the additive is an antistatic agent; Preferably, the dosage of the additive is 1-3 mg / L.

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