Method for producing No.3 crude white oil

Abstract

The invention relates to a method for producing No.3 crude white oil, which comprises the following steps of: processing raw materials with high impurity content by adopting a single-stage, high-pressure and light oil type hydrocracking technology, optimizing process parameters of a hydrocracking device to improve the product quality of distillate aviation fuel and diesel oil, and blending the aviation fuel and the diesel oil according to a certain proportion to obtain the No.3 crude white oil. And a No.3 crude white oil product meeting the quality standard of crude white oil (NB / SH / T0914-2019) is produced. When the fuel oil is not smoothly sold in the market, special products are produced, the product structure is optimized, the added value of the products is improved, the production and operation pressure of refinery plants is relieved, and the low-carbon, green and transformation and upgrading development requirements of refinery enterprises are met.

Description

Technical Field

[0001] The invention relates to a method for producing No. 3 crude white oil, and belongs to the field of petroleum refining. Background Art

[0002] Adjusting the ratio of oil products and chemical products, converting more oil products into aromatics, olefins and specialty products, and further extending the industrial chain downstream to produce high value-added products is one of the important ways for the green and low-carbon development and transformation and upgrading of the refining and chemical industry.

[0003] Hydrocracking technology can process a variety of conventional raw materials (wax oil, diesel, etc.) and unconventional raw materials; the process flow is diverse and the catalyst system is highly targeted, which can provide the best technical route for the different production needs of enterprises; the product variety is flexible and varied with excellent quality, which can achieve a variety of production plans such as high-yield chemical raw materials, high-yield jet fuel, high-yield intermediate distillates and high-yield tail oil, providing strong technical support for refining enterprises to adjust their product structure and continue to develop at a high speed.

[0004] Crude white oil is the raw material for producing industrial white oil, cosmetic white oil and other finished white oils. Crude white oil can be obtained through deep hydrogenation and fraction cutting. Finished white oil is widely used in industrial production, cosmetics, food and medicine. With the development of the economy and the improvement of living standards, people's consumption demand and quality requirements for white oil products are gradually increasing. As one of the raw materials for the production of white oil products, the properties of crude white oil are closely related to the quality of white oil products. In order to ensure the stability of the quality of finished white oil, the National Energy Administration promulgated the "Crude White Oil" (NB / SH / T0914-2019) quality standard in June 2019, which brought certain challenges to companies producing crude white oil.

[0005] CN 107987881 A discloses a method for preparing crude white oil. It comprises the following steps: 1) mixing furfural extracted oil with light fraction oil to obtain raw oil; 2) heating the raw oil, and then the heated raw oil enters a series hydrogenation reaction device for hydrogenation reaction to obtain a product; the series hydrogenation reaction device is composed of a first-stage reactor and a second-stage reactor; 3) the product prepared in step 2) is fraction cut, and after the light fraction is cut off, the crude white oil is obtained. The preparation method of the present invention has better adaptability to raw materials, can obtain a higher product yield while ensuring product quality, and the raw oil contains a certain amount of low-value-added furfural extracted oil, which can significantly improve the overall processing efficiency. According to the analysis of the patent publication data, the crude white oil produced by this method meets the quality standard of No. 5 crude white oil, wherein the kinematic viscosity (40°C): 4.165.06 (mm 2 ·s -1 ), grade sulfur content: 2.9~9.8≤10(mg·kg-1 ).

[0006] CN 109722300 A discloses a hydrogenation method for producing crude white oil, comprising: heavy raw oil and hydrogen-containing streams are mixed and sequentially passed through a hydrorefining reaction zone I, a hydrocracking reaction zone and a hydrorefining reaction zone II for reaction, the reaction effluent is separated and fractionated to obtain a crude white oil product with qualified properties, the hydrorefining reaction zone I is filled with a hydrorefining catalyst I, the hydrocracking reaction zone is filled with a hydrocracking catalyst, and the hydrorefining reaction zone II is filled with a hydrorefining catalyst II. Technical comparison: This method adopts a method of grading three hydrogenation reaction zones and three hydrogenation catalysts together, wherein the hydrorefining reaction zone I is filled with a hydrorefining catalyst I, the hydrocracking reaction zone is filled with a hydrocracking catalyst, and the hydrorefining reaction zone II is filled with a hydrorefining catalyst II, and the process of this method is relatively complicated. The closed cup flash point of the No. 3 crude white oil of this method is about 50°C, which does not meet the quality standard of more than 65°C, and the aromatic mass fraction of Example 1 is 13.8%, which does not meet the requirements.

[0007] The method comprises: mixing heavy crude oil and hydrogen-containing streams and sequentially passing through a hydrofining reaction zone and a hydrocracking reaction zone, separating and fractionating the reaction effluent to obtain a crude white oil product with qualified properties, loading the hydrofining reaction zone with a hydrofining catalyst, and sequentially loading the hydrocracking reaction zone with a hydrocracking catalyst I and a hydrocracking catalyst II. The method of the present invention not only broadens the raw material source for producing white oil, but also effectively reduces the investment cost and operating cost of the device. The quality standard of the aromatic mass fraction of the No. 3 crude white oil of the method is not met at 10.3-13.5.

[0008] CN 110041964 A discloses a method for producing a crude white oil product, comprising the following steps: a) mixing the raw oil with hydrogen, heating it to 300°C to 320°C, and then entering the first reactor for a hydrofining reaction, controlling the temperature rise to 30°C to 60°C to obtain a refined reaction product; the raw oil is composed of a normal pressure diesel fraction and a coking diesel fraction in a mass ratio of (1 to 6): 4; b) the refined reaction product obtained in step a) enters the second reactor for a diesel reforming reaction, controlling the temperature rise to 5°C to 20°C to obtain a reforming reaction product; c) the reforming reaction product obtained in step b) is subjected to gas-liquid separation, and the obtained gas is desulfurized and recycled; the obtained liquid is fractionated to obtain naphtha and crude white oil, respectively. The mass fraction of aromatics in the No. 3 crude white oil of the method is 12.2 to 13.8%, which does not meet the standard of less than 10% of the crude white oil NB / SH / T 0914-2019 standard. At the same time, the raw material of this method is light distillate oil, and it is easier to produce crude white oil.

[0009] CN 110616084 AThe present disclosure relates to a method for producing crude white oil, which comprises the following steps: a. allowing a coal tar fraction to enter a hydrorefining reaction zone and contact a hydrorefining catalyst to perform a hydrorefining reaction to obtain a hydrorefining product, and separating the hydrorefining product to obtain naphtha, a first crude white oil, and a first hydrogenated tail oil; b. allowing at least part of the first hydrogenated tail oil to enter a hydrocracking reaction zone and contact a hydrocracking catalyst to perform a hydrocracking reaction to obtain a hydrocracking product, and separating the hydrocracking product to obtain naphtha, a second crude white oil, and a second hydrogenated tail oil. The method can convert low-quality and cheap coal tar fractions into high-value-added crude white oil products. The mass fraction of aromatics in the No. 3 crude white oil of the method is 11.5-13.2%, and the closed-mouth flash is about 50°C, which does not meet the crude white oil NB / SH / T0914-2019 standard. At the same time, the method is a two-stage hydrogenation process, and the operation process is complicated.

[0010] CN 110616083 A The present invention relates to a method for producing crude white oil, which comprises the following steps: a. allowing inferior coal tar to enter a hydrorefining reaction zone for hydrorefining reaction to obtain a hydrorefining product, and separating the hydrorefining product to obtain naphtha, a first diesel and a first hydrorefining tail oil; dividing the first hydrorefining tail oil into a first part of the first hydrorefining tail oil and a second part of the first hydrorefining tail oil; b. allowing the first part of the first hydrorefining tail oil to enter a first hydrocracking reaction zone and contact with a first hydrocracking catalyst to perform a first hydrocracking reaction; the first hydrocracking catalyst contains a Y-type molecular sieve; c. allowing the second part of the first hydrorefining tail oil to enter a second hydrocracking reaction zone and contact with a second hydrocracking catalyst to perform a second hydrocracking reaction; the second hydrocracking catalyst contains a β-type molecular sieve. The method can convert inferior and cheap coal tar into a high value-added crude white oil product. The mass fraction of aromatics in the No. 3 crude white oil of this method is 8.5-10.5%, which does not fully meet the crude white oil NB / SH / T 0914-2019 standard. In addition, this method has a complex two-stage hydrogenation process and high operating costs.

[0011] There are currently reported technical problems with the production technology for producing No. 3 crude white oil: it does not meet the requirements of the crude white oil standard NB / SH / T0914-2019, such as flash point and aromatic mass fraction; it can only process high-quality raw materials or use a complex two-stage hydrogenation technology. Summary of the invention

[0012] The object of the present invention is to provide a method for producing No. 3 crude white oil, which adopts a single-stage, high-pressure, light oil-type hydrocracking technology to process inferior raw materials with high impurity content, optimizes the process parameters of the hydrocracking unit, improves the product flash point and aromatic mass fraction index of distillate oil jet fuel and diesel, and blends jet fuel and diesel in a certain proportion to achieve the purpose of producing a No. 3 crude white oil product that meets the quality standard of "Crude White Oil" (NB / SH / T0914-2019).

[0013] The object of the invention is achieved in this way: The method for producing No. 3 crude white oil of the present invention comprises the following steps: using a hydrocracking device to process inferior raw materials by adopting a single-stage, high-pressure, light oil type hydrocracking technology, optimizing process parameters, improving the properties of diesel and aviation kerosene products, and blending aviation kerosene and diesel in a certain proportion to produce No. 3 crude white oil that meets the new standards.

[0014] The method for producing No. 3 crude white oil of the present invention comprises the hydrocracking technology being a high-pressure hydrocracking technology and the operating pressure being 14.7 MPa.

[0015] The method for producing No. 3 crude white oil of the present invention, the light oil type hydrocracking technology, the light oil yield is greater than 50%.

[0016] The method for producing No. 3 crude white oil of the present invention comprises the following steps: the raw material of the hydrocracking unit is vacuum wax oil produced by a normal vacuum device using Shaqing light, Shazhong and Kuwait crude oil as raw materials; Shaqing light, Shazhong and Kuwait crude oil are high-sulfur intermediate base crude oils; the sulfur content of the vacuum wax oil is about 3% by mass, the nitrogen content is about 1000 mg / kg, the aromatics + colloid content is about 44% by mass, and the impurity content is high, so the vacuum wax oil is an inferior raw material for producing crude white oil.

[0017] In the method for producing No. 3 crude white oil of the present invention, the hydrorefining catalyst used in the hydrocracking unit is HYT-6219-1.3T or KF-848-1.3Q, and the hydrocracking catalyst is HC-24L or HC-120.

[0018] The method for producing No. 3 crude white oil of the present invention comprises the following main process parameters of the hydrocracking unit: a hydrogen-to-oil ratio greater than 1137, a refining reaction temperature of 350-390°C, and a cracking reaction temperature of 350-400°C.

[0019] The method for producing No. 3 crude white oil of the present invention controls the distillation range of the aviation kerosene product of the hydrocracking unit to be between 185 and 260°C; and controls the distillation range of the diesel product to be between 200 and 360°C.

[0020] The method for producing No. 3 crude white oil of the present invention adopts a blending method to produce No. 3 crude white oil products, wherein diesel products of a hydrocracking unit and aviation kerosene products are blended at a weight ratio of 0.3 to 1.5 to produce No. 3 crude white oil products that meet new standards.

[0021] The No. 3 crude white oil produced by the method for producing No. 3 crude white oil of the present invention has a product quality that meets the quality index of No. 3 crude white oil, wherein the kinematic viscosity (40°C) is 1 to <3 (mm 2 ·s-1), closed cup flash point: ≥65℃, color / Saybolt color number: ≥20, copper sheet corrosion (50℃, 3h): ≤1, grade sulfur content: ≤10 (mg·kg-1), aromatic mass fraction: ≤10%.

[0022] The hydrocracking unit uses vacuum wax oil as raw material, and its main products are crude liquefied gas, light naphtha, heavy naphtha, jet fuel and diesel, etc. Jet fuel and diesel with similar indicators to No. 3 crude white oil were selected for comparative analysis. The properties of jet fuel and diesel in the hydrocracking unit are shown in Table 1: Table 1 Comparison of properties of jet fuel and diesel with crude white oil project <![CDATA[3# White Mineral Oil * > Jet fuel diesel fuel <![CDATA[Kinematic viscosity (40 °C) / (mm 2 ·s -1 )]]> 1～<3 1.707 4.772 Open flash point / ℃ 91 Closed cup flash point / ℃ ≥65 48 Color / Saybolt color number ≥20 30 22 Copper strip corrosion (50 ℃, 3 h) / level ≤1 Level 1a Level 1a <![CDATA[Sulfur content / (mg·kg -1 )]]> ≤10 ≤1 ≤1 Aromatics mass fraction / % ≤10 12.8 7.2 <![CDATA[Nitrogen content / (mg·kg -1 )]]> ≤100 ≤1 ≤1 * Data from standard NB / SH / T 0914-2019 Compared with the standard of No. 3 crude white oil, the flash point of aviation kerosene is low, the mass fraction of aromatics is high, and other properties meet the index requirements; the kinematic viscosity of diesel is high, and other properties meet the index requirements. Therefore, improving the closed cup flash point of aviation kerosene, reducing the mass fraction of aromatics in aviation kerosene, or reducing the kinematic viscosity of diesel products is the working direction of the hydrocracking unit to produce No. 3 crude white oil. Especially during the epidemic, the market demand for fuel oil products such as aviation kerosene and diesel has dropped significantly. The production of No. 3 crude white oil with aviation kerosene and diesel can alleviate the situation of poor sales of fuel oil, and its significance and role are particularly important. The method of the present invention improves the reaction depth: improving the reaction depth is conducive to the reaction of hydrodesulfurization, hydrodenitrogenation, aromatic saturation and the like. Therefore, in order to reduce the aromatic mass fraction of aviation kerosene and diesel products, the average temperature of the refining and cracking beds is increased, that is, the reaction depth is increased. In order to increase the flash point of aviation kerosene and diesel, the process parameters of the fractionation system are adjusted, including increasing the top temperature of the fractionation tower, increasing the bottom temperature of the aviation kerosene tower, and increasing the steam volume of the diesel tower stripping. Optimize the distillation range of oil products: The mass fraction of aromatics in the light part of jet kerosene is relatively high, and the mass fraction of aromatics in jet kerosene is also higher than that in diesel. It can be concluded that aromatics are concentrated in the lighter parts of jet kerosene and diesel. Therefore, separating the lighter components of jet kerosene and diesel is conducive to controlling the mass fraction of aromatics in jet kerosene and diesel. Although the indicators of jet kerosene and diesel have been improved, the mass fraction of aromatics in jet kerosene and the kinematic viscosity of diesel do not meet the indicators of No. 3 crude white oil. By blending jet kerosene and diesel, the goal of producing No. 3 crude white oil can be achieved. Using the existing diesel blending system, jet kerosene and diesel are produced and blended in a certain proportion to produce qualified No. 3 crude white oil products.

[0023] The present invention uses high-sulfur intermediate-base Middle East crude oil as raw material, adopts single-stage full-cycle hydrocracking technology, optimizes the process parameters of the hydrocracking unit, improves the product indicators of aviation kerosene and diesel, determines the blending ratio of aviation kerosene and diesel through blending tests, and produces No. 3 crude white oil products. This method can optimize the product structure, increase the added value of the product, and meet the low-carbon, green, transformation and upgrading development needs of refining enterprises.

[0024] Effects of the present invention: (1) In refineries using Saudi Light, Saudi Medium and Kuwait Intermediate crude oil as raw materials, the hydrocracking unit processes raw materials with high sulfur, high nitrogen and high aromatic impurity content to produce qualified No. 3 crude white oil and develop new products.

[0025] (2) Under the premise of processing inferior raw materials, single-stage hydrocracking technology is used to produce No. 3 crude white oil.

[0026] (3) Without modifying the unit, by optimizing the process parameters, the quality of the unit's distillate oil products can be improved, so that the hydrocracking jet fuel and diesel product indicators meet or approach the quality standards of No. 3 crude white oil, and serve as the blending base oil for No. 3 crude white oil.

[0027] (4) Without building a new unit, the blending ratio of jet fuel and diesel in the hydrocracking unit is determined through blending tests to meet the quality standards of No. 3 crude white oil and achieve the purpose of producing No. 3 crude white oil.

[0028] (5) When fuel oil sales are sluggish in the market, we produce special products, optimize the product structure, and alleviate the production and operation pressure of refineries.

[0029] (6) Produce No. 3 crude white oil and develop special products in line with the low-carbon, green, transformation and upgrading development needs of refining and chemical companies. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 It is a process flow chart of the present invention. DETAILED DESCRIPTION

[0031] Figure 1 Among them, vacuum wax oil 1, new hydrogen 2, circulating oil 3, raw oil buffer tank 4, reaction feed pump 5, circulating hydrogen 6, reaction feed heating furnace 7, hydrotreating reactor 8, hydrocracking reactor 9, circulating hydrogen compressor 10, hot high fraction 11, hot low fraction 12, cold high fraction 13, cold low fraction 14, stripping tower 15, pre-flash tank 16, distillation heating furnace feed pump 17, distillation feed heating furnace 18, distillation tower 19, naphtha 20, jet fuel 21, diesel 22, and tail oil 23.

[0032] The method for producing No. 3 crude white oil is implemented without changing the process flow of the original hydrocracking unit. The process flow is as follows: the vacuum wax oil enters the raw oil tank for mixing, is pressurized by the reaction feed pump, and is heated by the reaction feed heating furnace before entering the refining and cracking reactor for reaction. The reaction product is heated by the fractionation heating furnace and then enters the fractionation tower for separation to produce naphtha, jet fuel, diesel and other products.

[0033] The vacuum wax oil 1 enters the crude oil buffer tank 4 as the raw material of the hydrocracking unit. The crude oil is pressurized to 18.0MPa by the reaction feed pump 5 and mixed with circulating hydrogen (hydrogen-oil ratio is greater than 1137). After being heated to 350-370°C by the reaction feed heating furnace 7, it enters the hydrofining reactor 8 for desulfurization, denitrogenation, dearomatization and other reactions, and the refining reaction temperature is 350-390°C; then it enters the hydrocracking reactor 9 for cracking reaction, and the cracking reaction temperature is 350-400°C. After the reaction product is separated into gas and liquid by the high-low pressure separator and the stripping tower 15, the bottom oil of the stripping tower 15 is heated to 350-370°C by the fractionation feed heating furnace 18, and then enters the fractionation tower 19 for separation, producing naphtha 20, jet fuel 21, and diesel product 22.

[0034] Optimize the process parameters of the hydrocracking unit, improve the product indicators of jet fuel and diesel, determine the blending ratio of jet fuel and diesel through blending tests, and produce No. 3 crude white oil product.

[0035] The hydrocracking unit uses vacuum wax oil as raw material, with a processing capacity of 130t / h. A test of producing No. 3 crude white oil was carried out. The specific implementation steps are as follows: Reaction section adjustment: (1) Keep the total feed of the unit at 130t / h, increase the temperature of the refining reactor at a rate of 0.2℃ / time, and control the operating conditions as follows: reaction pressure 14.7MPa, average refining reaction temperature 360℃, average cracking reaction temperature 353~355℃, hydrogen-oil volume ratio 1160, refining reactor 8 single bed temperature rise ≤42℃, cracking reactor 9 single bed temperature rise ≤28℃, cold hydrogen valve opening ≤65%, high and low liquid separation tanks, stripping tower 15, fractionation tower 19 liquid level controlled at 55%, fractionation feed heating furnace 18 outlet temperature controlled at 360℃. Appropriately adjust the cracking reaction temperature to stabilize the reaction depth, maintain the heavy naphtha yield at 36%, and operate stably for 24 hours. Contact the laboratory for sampling and analysis of the product properties of jet fuel 21 and diesel 22 of the hydrocracking unit.

[0036] (2) Maintain the total feed of the unit at 130t / h, increase the temperature of the refining reactor at a rate of 0.2℃ / time, and control the operating conditions as follows: reaction pressure 14.7MPa, average refining reaction temperature 362℃, average cracking reaction temperature 353~355℃, hydrogen-oil volume ratio 1160, refining reactor 8 single bed temperature rise ≤42℃, cracking reactor 9 single bed temperature rise ≤28℃, cold hydrogen valve opening ≤65%, high and low liquid separation tanks, stripping tower 15, fractionation tower 19 liquid level controlled at 55%, fractionation feed heating furnace 18 outlet temperature controlled at 360℃. Appropriately adjust the cracking reaction temperature to stabilize the reaction depth, maintain the heavy naphtha yield at 36%, and operate stably for 24 hours. Contact the laboratory for sampling and analysis of the product properties of jet fuel 21 and diesel 22 of the hydrocracking unit.

[0037] (3) Maintain the total feed of the unit at 130t / h, increase the temperature of the refining reactor at a rate of 0.2℃ / time, and control the operating conditions as follows: reaction pressure 14.7MPa, average refining reaction temperature 364℃, average cracking reaction temperature 353~355℃, hydrogen-oil volume ratio 1160, refining reactor 8 single bed temperature rise ≤42℃, cracking reactor 9 single bed temperature rise ≤28℃, cold hydrogen valve opening ≤65%, high and low liquid separation tanks, stripping tower 15, fractionation tower 19 liquid level controlled at 55%, fractionation feed heating furnace 18 outlet temperature controlled at 360℃. Appropriately adjust the cracking reaction temperature to stabilize the reaction depth, maintain the heavy naphtha yield at 36%, and operate stably for 24 hours. Contact the laboratory to sample and analyze the product properties of the hydrocracking unit jet fuel 21 and diesel 22. When the aromatics, color, sulfur, and nitrogen content of the jet fuel and diesel products do not change much, stop heating.

[0038] Fractionation tower process adjustment: (4) Maintain the total feed rate of the unit at 130 t / h, increase the top temperature of the fractionator 19 at a rate of 1°C / time, and control the operating conditions to: top temperature of the fractionator 126°C, fractionator stripping steam flow rate 12.4 t / h, top pressure of the fractionator 0.06 MPa, and outlet temperature of the fractionator feed heater 18 at 360°C. Operate stably for 24 hours. Contact the laboratory for sampling and analysis of the properties of the jet fuel and diesel products of the hydrocracking unit.

[0039] (5) Maintain the total feed of the unit at 130 t / h, increase the top temperature of the fractionator at a rate of 1°C / time, and control the operating conditions as follows: top temperature of the fractionator at 128°C, steam flow of the fractionator stripping at 12.4 t / h, top pressure of the fractionator at 0.06 MPa, and outlet temperature of the fractionator feed heater 8 at 360°C. Operate stably for 24 hours. Contact the laboratory for sampling and analysis of the properties of the jet fuel and diesel products of the hydrocracking unit.

[0040] (6) Keep the total feed of the unit at 130t / h, increase the top temperature of the fractionator at a rate of 1℃ / time, and control the operating conditions as follows: top temperature of the fractionator at 130℃, steam flow of the fractionator stripping at 12.4t / h, top pressure of the fractionator at 0.06MPa, and outlet temperature of the fractionation feed heating furnace 18 at 360℃. Operate stably for 24 hours. Contact the laboratory to sample and analyze the properties of the jet fuel and diesel products of the hydrocracking unit. When the flash point of the jet fuel and diesel products meets the No. 3 white oil standard, stop heating.

[0041] Diesel tower operation adjustments: (7) Maintain the total feed of the unit at 130 t / h, increase the steam volume of the diesel tower stripping at a rate of 0.5 t / h, and control the operating conditions as follows: the top temperature of the fractionation tower 19 is 130°C, the steam flow rate of the fractionation tower stripping is 12.4 t / h, the pressure of the fractionation tower is 0.06 MPa, the outlet temperature of the fractionation feed heating furnace 18 is controlled at 360°C, and the steam volume of the diesel tower stripping is 1 t / h. Stable operation for 24 hours. Contact the laboratory for sampling and analysis of the properties of the jet fuel and diesel products of the hydrocracking unit.

[0042] (8) Keep the total feed of the unit at 130 t / h, increase the steam volume of the diesel tower at a rate of 0.5 t / h, and control the operating conditions as follows: the top temperature of the fractionation tower is 130°C, the steam flow rate of the fractionation tower is 12.4 t / h, the top pressure of the fractionation tower is 0.06 MPa, the outlet temperature of the fractionation feed heating furnace 18 is controlled at 360°C, and the steam volume of the diesel tower is 2 t / h. Stable operation for 24 hours. Contact the laboratory to sample and analyze the product properties of the jet fuel and diesel in the hydrocracking unit. When the flash point of the diesel does not change much, stop increasing the steam volume of the diesel tower.

[0043] (9) Analytical testing for blending test: (10) Carry out blending tests according to the No. 3 crude white oil index standard to determine the blending ratio of aviation kerosene and diesel.

[0044] (11) The storage and transportation department conducts blending production: (12) The Storage and Transportation Department shall carry out the production and blending of No. 3 crude white oil in accordance with the blending ratio determined by the Laboratory and produce qualified No. 3 white oil products.

[0045] (13) The properties of diesel and jet fuel before and after the adjustment are compared as follows: (14) The wax oil hydrocracking unit has improved the flash point and aromatic mass fraction of jet fuel and diesel by increasing the reaction depth, increasing the flash point, and optimizing the oil distillation range. Other property indicators have not changed much. See Table 2 for details.

[0046] Table 2 Properties of jet fuel and diesel before and after optimization project Jet fuel (before adjustment) Jet fuel (adjusted) Diesel (before adjustment) Diesel (adjusted) <![CDATA[Kinematic viscosity (40 °C) / (mm 2 ·s -1 )]]> 1.707 1.776 4.772 4.872 Open flash point / ℃ 91 125 Closed cup flash point / ℃ 48 69 Color / Number 30 30 22 30 Aromatics mass fraction / % 12.8 11.2 7.2 6.5 From the table above, we can see that although the indicators of jet fuel and diesel have been improved, the aromatic mass fraction and kinematic viscosity of jet fuel still do not meet the indicators of No. 3 crude white oil. By blending jet fuel and diesel, the goal of producing No. 3 crude white oil can be achieved. The company uses the existing diesel blending system to produce and blend jet fuel and diesel in a certain proportion to produce qualified No. 3 crude white oil products. The indicators of No. 3 crude white oil products are shown in Table 3: Table 3 Properties of No. 3 crude white oil product after process parameter adjustment project No. 3 crude white oil standard No. 3 white oil product (product 1) No. 3 white oil product (product 2) <![CDATA[Kinematic viscosity (40 °C) / (mm 2 ·s -1 )]]> 1～<3 2.484 2.150 Closed cup flash point / ℃ ≥65 71 68 Color / Number ≥20 30 30 Copper strip corrosion (50 ℃, 3 h) / level 0≤1 1a 1a <![CDATA[Sulfur content / (mg·kg -1 )]]> ≤10 ≤1 ≤1 Aromatics mass fraction / % ≤1 9.5 8.9 <![CDATA[Nitrogen content / (mg·kg -1 )]]> ≤100 ≤1 ≤1

Claims

1. A method for producing No. 3 crude white oil, characterized in that: The method is to use a hydrocracking unit with single-stage, high-pressure, light oil-type hydrocracking technology to process inferior raw materials, improve the properties of diesel and jet fuel products by optimizing process parameters, and produce No. 3 crude white oil that meets the new standards by blending jet fuel and diesel in a certain proportion.

2. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The hydrocracking technology is a high-pressure hydrocracking technology with an operating pressure of 14.7 MPa.

3. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The light oil type hydrocracking technology has a light oil yield greater than 50%.

4. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The raw material of the hydrocracking unit is vacuum wax oil produced by a normal vacuum unit using Shaqing Light, Shazhong and Kuwait crude oil as raw materials; Shaqing Light, Shazhong and Kuwait crude oil are high-sulfur intermediate base crude oils; the sulfur content of the vacuum wax oil is about 3%, the nitrogen content is about 1000 mg / kg, the aromatics + gum content is about 44%, and the impurity content is high, so it is an inferior raw material for producing crude white oil.

5. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The hydrorefining catalyst used in the hydrocracking unit is HYT-6219-1.3T and KF-848-1.3Q, and the hydrocracking catalyst is HC-24L and HC-120.

6. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The main process parameters of the hydrocracking unit are: hydrogen-to-oil ratio greater than 1137, refining reaction temperature of 350-390°C, and cracking reaction temperature of 350-400°C.

7. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The distillation range of the jet fuel product of the hydrocracking unit is controlled at 185-260°C; the distillation range of the diesel product is controlled at 200-360°C.

8. The method for producing No. 3 crude white oil as claimed in claim 1, characterized in that: The No. 3 crude white oil product is produced by a blending method, in which the diesel product of the hydrocracking unit and the aviation kerosene product are blended in a weight ratio of 0.3 to 1.5 to produce a No. 3 crude white oil product that meets the new standards.

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