A low-sulfur high-performance fuel oil production device

Abstract

The present application relates to a kind of low sulfur high performance fuel oil production device, it relates to fuel oil production technical field.Low sulfur modified residual oil, hydrogenation low sulfur raffinate are used as main raw material, auxiliary agent A, auxiliary agent B prepared by special oil device are matched, reaction conditions are accurately controlled through DCS system, low sulfur high performance marine fuel oil is prepared in low temperature mild environment;Device integrates vacuum deep pull and viscosity reduction cracking combined process, light fraction can be deep-processed into three kinds of base oil, etc.Additional value products, heavy fraction is reduced in viscosity by viscosity reduction cracking, and low-temperature fluidity is improved;Auxiliary agent B is prepared by dithiophosphoric acid, molybdenum trioxide, epoxy succinic acid polymer, 2,6-naphthalene dicarboxylic acid, anhydrous toluene, phosphorous acid;Fuel oil prepared by the present application, sulfur content is lower, environmental protection is better, low-temperature fluidity is improved, and combustion efficiency is better.

Description

Technical Field

[0001] This invention relates to the field of fuel oil production technology, and in particular to a low-sulfur, high-performance fuel oil production apparatus. Background Technology

[0002] Currently, with improved environmental regulations, most passenger vehicles are transitioning from traditional internal combustion engines to new energy vehicles to reduce emissions. However, the marine sector still relies heavily on internal combustion engines, with marine fuel primarily consisting of heavy fuel oil. While heavy fuel oil is cheaper, it has a higher sulfur content. Currently, there are two main methods for addressing sulfur dioxide emissions in ships: one is to burn high-sulfur fuel oil and add desulfurization and denitrification systems to the emission control system to reduce emissions; the other is to directly purchase and use low-sulfur fuel oil to reduce emissions at the source. However, low-sulfur marine fuel oil is relatively expensive and has a lower calorific value.

[0003] Chinese Patent CN103958648B: This invention relates to a method for converting petroleum feedstock to produce low-sulfur fuel oil. The method includes the following sequential steps: a step of performing fixed-bed hydrodemetallization on the feedstock using an upstream system of a swing-type fixed-bed reactor; a step of performing fixed-bed hydrocracking on the hydrodemetallized effluent in the presence of a hydrocracking catalyst; a separation step to obtain a heavy fraction; and a step of hydrodesulfurizing the heavy fraction, in which hydrogen is reinjected.

[0004] Chinese Patent CN112708460A: A method for producing low-carbon olefins and low-sulfur fuel oil components, wherein the feedstock oil is reacted in contact with a catalyst in a catalytic conversion reactor, characterized by a reaction temperature, weight hourly space velocity, and a catalyst-to-feedstock oil weight ratio sufficient to produce reaction products comprising 8-25 wt% propylene and 15-50 wt% catalytic cracking distillate oil, wherein the catalytic cracking distillate oil is hydrodesulfurized to obtain low-sulfur hydrotreated distillate oil as a fuel oil component.

[0005] Low-sulfur fuel oil produced by existing technologies suffers from problems such as high price, low calorific value, and poor low-temperature fluidity. Summary of the Invention

[0006] To address the aforementioned problems, this invention provides a low-sulfur, high-performance fuel oil production apparatus, comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0007] In some embodiments, the raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The amounts added to the four feed lines are respectively: 35-65 parts of low-sulfur modified residue oil, 15-30 parts of hydrotreated low-sulfur raffinate oil, 0.03-0.3 parts of additive A, and 0.02-0.2 parts of additive B.

[0008] In some embodiments, the additive A is composed of 20-40 parts of ethylene-vinyl acetate copolymer, 17-35 parts of polymethacrylate, and 15-25 parts of alkylnaphthalene.

[0009] In some embodiments, the preparation method of the auxiliary agent B is as follows: By weight, 20-40 parts of dithiophosphoric acid, 7-14 parts of molybdenum trioxide, 0.5-2 parts of epoxy succinic acid polymer, 0.2-0.5 parts of 2,6-naphthalenedicarboxylic acid, 200-300 parts of anhydrous toluene, and 2-5 parts of phosphorous acid are mixed and then the air in the reactor is replaced with nitrogen 3-5 times. The temperature is raised to 85-100℃ and the reaction is carried out for 1-4 hours, with the stirring rate controlled at 200-350 r / min throughout the process. After the reaction is completed, toluene is removed by vacuum distillation under negative pressure conditions of 70-85℃ and 0.075-0.09 MPa to obtain auxiliary agent B.

[0010] In some embodiments, the free acid value is detected by sampling during the reaction process, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0011] In some embodiments, the reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0012] In some embodiments, the reaction temperature of the reaction unit is 60-80°C, the reaction pressure is 0.3-0.5 MPa, and the residence time is 1-3 h.

[0013] In some embodiments, the product separation unit employs a vacuum deep-drawing technique, with a vacuum furnace outlet temperature of 410-430℃, an operating pressure of 2-3 kPa absolute pressure inside the column, and a bottom temperature of 345-365℃; separating light and heavy fractions.

[0014] In some embodiments, the light fraction produced by vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0015] In some embodiments, the heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 60-80℃, a pressure of 0.2-0.3MPa, and a residence time of 30-60min.

[0016] Reaction mechanism: Using low-sulfur modified residue oil and hydrotreated low-sulfur raffinate oil as main raw materials, and compounded with functional additives containing dithiophosphoric acid, molybdenum trioxide, and epoxy succinic acid polymers, the directional modification and molecular recombination of heavy components are completed under low-temperature and mild conditions. Dithiophosphoric acid and molybdenum trioxide form a highly efficient active coordination structure, which, together with the dispersing and stabilizing effect of epoxy succinic acid polymers, optimizes the colloidal state and low-temperature rheological behavior of heavy components, while reducing the sulfur content of the oil and improving combustion efficiency. Coupled with vacuum deep-drawing and viscosity-reducing cracking processes, the high-value-added light fraction and the upgrading of heavy fraction are achieved, forming a stable and efficient low-sulfur fuel oil system.

[0017] Technical effects: The present invention provides a low-sulfur, high-performance fuel oil production apparatus. Compared with the prior art, the present invention has the following significant advantages: 1. Dithiophosphoric acid and molybdenum trioxide form highly efficient active coordination compounds in situ, which can optimize the structure of heavy components, reduce oil viscosity and improve low-temperature fluidity.

[0018] 2. Epoxy succinic acid polymers play a dispersing, stabilizing, and detergency role, inhibiting component aggregation and ensuring long-term uniformity and stability of the oil. Naphthyl groups have a strong aromatic and regular structure, which can form stable associations with heavy hydrocarbons, significantly improving the low-temperature flow and low-temperature anti-flocculation properties of the oil.

[0019] 3. The three elements work synergistically to achieve integrated modification of low sulfur content, viscosity reduction, and efficiency improvement, significantly enhancing the environmental friendliness, fluidity, and combustion performance of fuel oil. Attached Figure Description

[0020] Figure 1 Flowchart of a low-sulfur, high-performance fuel oil production unit. Detailed Implementation

[0021] To further illustrate the technical means and effects of the present invention in achieving its intended purpose, the following detailed description of the specific implementation methods, structures, features, and effects of the present invention, in conjunction with the accompanying drawings and preferred embodiments, is provided below.

[0022] 1. Sulfur content detection: The sulfur content in petroleum and petroleum products shall be determined by energy dispersive X-ray fluorescence spectrometry in accordance with GB / T17040-2019. 2. Kinematic viscosity test: The test shall be performed in accordance with GB / T265-1988, the method for determining the viscosity of petroleum products. 3. Calorific value test: The calorific value shall be determined in accordance with GB / T384-1981, the method for determining the calorific value of petroleum products. Example 1

[0023] A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0024] The raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The feed amounts added to the four feed lines are: 35 kg of low-sulfur modified residue oil, 15 kg of hydrotreated low-sulfur raffinate oil, 0.03 kg of additive A, and 0.02 kg of additive B, respectively.

[0025] The additive A is composed of 20 kg of ethylene-vinyl acetate copolymer, 17 kg of polymethyl methacrylate, and 15 kg of alkylnaphthalene.

[0026] The preparation method of the aforementioned auxiliary agent B is as follows: 20 kg of dithiophosphoric acid, 7 kg of molybdenum trioxide, 0.5 kg of epoxy succinic acid polymer (CAS: 51274-37-4), 0.2 kg of 2,6-naphthalenedicarboxylic acid, 200 kg of anhydrous toluene, and 2 kg of phosphorous acid were mixed and then the air in the reactor was replaced three times with nitrogen gas. The mixture was heated to 85 °C and reacted for 1 hour, with the stirring rate controlled at 200 r / min throughout the process. After the reaction was completed, toluene was removed by vacuum distillation under 70 °C and 0.075 MPa negative pressure to obtain auxiliary agent B.

[0027] During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0028] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0029] The reaction unit has a reaction temperature of 60°C, a reaction pressure of 0.3 MPa, and a residence time of 1 h.

[0030] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 410℃, an operating pressure of 2kPa absolute pressure inside the column, and a bottom temperature of 345℃; it separates light and heavy fractions.

[0031] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0032] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 60℃, a pressure of 0.2MPa, and a residence time of 30min. Example 2

[0033] A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0034] The raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The feed amounts added to the four feed lines are: 45 kg of low-sulfur modified residue oil, 20 kg of hydrotreated low-sulfur raffinate oil, 0.1 kg of additive A, and 0.1 kg of additive B, respectively.

[0035] The additive A is composed of 25 kg of ethylene-vinyl acetate copolymer, 21 kg of polymethyl methacrylate, and 18 kg of alkylnaphthalene.

[0036] The preparation method of the aforementioned auxiliary agent B is as follows: 25 kg of dithiophosphoric acid, 9 kg of molybdenum trioxide, 1 kg of epoxy succinic acid polymer (CAS: 51274-37-4), 0.3 kg of 2,6-naphthalenedicarboxylic acid, 240 kg of anhydrous toluene, and 3 kg of phosphorous acid were mixed and then the air in the reactor was replaced with nitrogen four times. The mixture was heated to 90 °C and reacted for 2 h, with the stirring rate controlled at 250 r / min throughout the process. After the reaction was completed, toluene was removed by vacuum distillation under 75 °C and 0.08 MPa negative pressure to obtain auxiliary agent B.

[0037] During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0038] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0039] The reaction unit has a reaction temperature of 65°C, a reaction pressure of 0.4 MPa, and a residence time of 2 hours.

[0040] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 415℃, an operating pressure of 2.5 kPa absolute pressure inside the column, and a bottom temperature of 350℃; it separates light and heavy fractions.

[0041] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0042] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 65℃, a pressure of 0.25MPa, and a residence time of 40min. Example 3

[0043] A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0044] The raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The feed amounts added to the four feed lines are: 55 kg of low-sulfur modified residue oil, 25 kg of hydrotreated low-sulfur raffinate oil, 0.2 kg of additive A, and 0.15 kg of additive B, respectively.

[0045] The additive A is composed of 35 kg of ethylene-vinyl acetate copolymer, 30 kg of polymethacrylate, and 23 kg of alkylnaphthalene.

[0046] The preparation method of the aforementioned auxiliary agent B is as follows: 35 kg of dithiophosphoric acid, 12 kg of molybdenum trioxide, 1.5 kg of epoxy succinic acid polymer (CAS: 51274-37-4), 0.4 kg of 2,6-naphthalenedicarboxylic acid, 280 kg of anhydrous toluene, and 4 kg of phosphorous acid were mixed and then the air in the reactor was replaced with nitrogen four times. The mixture was heated to 95 °C and reacted for 3 h, with the stirring rate controlled at 300 r / min throughout the process. After the reaction was completed, toluene was removed by vacuum distillation under 80 °C and 0.085 MPa negative pressure to obtain auxiliary agent B.

[0047] During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0048] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0049] The reaction unit has a reaction temperature of 75°C, a reaction pressure of 0.4 MPa, and a residence time of 2 hours.

[0050] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 425℃, an operating pressure of 2.5 kPa absolute pressure inside the column, and a bottom temperature of 360℃; it separates light and heavy fractions.

[0051] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0052] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 75℃, a pressure of 0.25MPa, and a residence time of 50min. Example 4

[0053] A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0054] The raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The feed amounts added to the four feed lines are: 65 kg of low-sulfur modified residue oil, 30 kg of hydrotreated low-sulfur raffinate oil, 0.3 kg of additive A, and 0.2 kg of additive B, respectively.

[0055] The additive A is composed of 40 kg of ethylene-vinyl acetate copolymer, 35 kg of polymethacrylate, and 25 kg of alkylnaphthalene.

[0056] The preparation method of the aforementioned auxiliary agent B is as follows: 40 kg of dithiophosphoric acid, 14 kg of molybdenum trioxide, 2 kg of epoxy succinic acid polymer (CAS: 51274-37-4), 0.5 kg of 2,6-naphthalenedicarboxylic acid, 300 kg of anhydrous toluene, and 5 kg of phosphorous acid were mixed and then the air in the reactor was replaced with nitrogen five times. The mixture was heated to 100 °C and reacted for 4 hours, with the stirring rate controlled at 350 r / min throughout the process. After the reaction was completed, toluene was removed by vacuum distillation under 85 °C and 0.09 MPa negative pressure to obtain auxiliary agent B.

[0057] During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0058] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0059] The reaction unit has a reaction temperature of 80℃, a reaction pressure of 0.5MPa, and a residence time of 3h.

[0060] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 430℃, an operating pressure of 3kPa absolute pressure inside the column, and a bottom temperature of 365℃; it separates light and heavy fractions.

[0061] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0062] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 80℃, a pressure of 0.3MPa, and a residence time of 60min.

[0063] Comparative Example 1 A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0064] The raw material pretreatment unit is connected to three feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, and additive A. The feed amounts added to the four feed lines are: 35 kg of low-sulfur modified residue oil, 15 kg of hydrotreated low-sulfur raffinate oil, and 0.03 kg of additive A, respectively.

[0065] The additive A is composed of 20 kg of ethylene-vinyl acetate copolymer, 17 kg of polymethyl methacrylate, and 15 kg of alkylnaphthalene.

[0066] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0067] The reaction unit has a reaction temperature of 60°C, a reaction pressure of 0.3 MPa, and a residence time of 1 h.

[0068] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 410℃, an operating pressure of 2kPa absolute pressure inside the column, and a bottom temperature of 345℃; it separates light and heavy fractions.

[0069] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0070] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 60℃, a pressure of 0.2MPa, and a residence time of 30min.

[0071] Comparative Example 2 A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0072] The raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The feed amounts added to the four feed lines are: 35 kg of low-sulfur modified residue oil, 15 kg of hydrotreated low-sulfur raffinate oil, 0.03 kg of additive A, and 0.02 kg of additive B, respectively.

[0073] The additive A is composed of 20 kg of ethylene-vinyl acetate copolymer, 17 kg of polymethyl methacrylate, and 15 kg of alkylnaphthalene.

[0074] The preparation method of the aforementioned auxiliary agent B is as follows: 7 kg of molybdenum trioxide, 0.5 kg of epoxy succinic acid polymer (CAS: 51274-37-4), 0.2 kg of 2,6-naphthalenedicarboxylic acid, 200 kg of anhydrous toluene, and 2 kg of phosphorous acid were mixed and then the air in the reactor was replaced three times with nitrogen gas. The mixture was heated to 85 °C and reacted for 1 hour, with the stirring rate controlled at 200 r / min throughout the process. After the reaction was completed, toluene was removed by vacuum distillation under 70 °C and 0.075 MPa negative pressure to obtain auxiliary agent B.

[0075] During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0076] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0077] The reaction unit has a reaction temperature of 60°C, a reaction pressure of 0.3 MPa, and a residence time of 1 h.

[0078] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 410℃, an operating pressure of 2kPa absolute pressure inside the column, and a bottom temperature of 345℃; it separates light and heavy fractions.

[0079] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0080] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 60℃, a pressure of 0.2MPa, and a residence time of 30min.

[0081] Comparative Example 3 A low-sulfur, high-performance fuel oil production device is characterized by comprising a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and upgrading unit, and a DCS automatic control unit.

[0082] The raw material pretreatment unit is connected to four feed lines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The feed amounts added to the four feed lines are: 35 kg of low-sulfur modified residue oil, 15 kg of hydrotreated low-sulfur raffinate oil, 0.03 kg of additive A, and 0.02 kg of additive B, respectively.

[0083] The additive A is composed of 20 kg of ethylene-vinyl acetate copolymer, 17 kg of polymethyl methacrylate, and 15 kg of alkylnaphthalene.

[0084] The preparation method of the aforementioned auxiliary agent B is as follows: 20 kg of dithiophosphoric acid, 0.5 kg of epoxy succinic acid polymer (CAS: 51274-37-4), 0.2 kg of 2,6-naphthalenedicarboxylic acid, 200 kg of anhydrous toluene, and 2 kg of phosphorous acid were mixed and then the air in the reactor was replaced three times with nitrogen gas. The mixture was heated to 85 °C and reacted for 1 hour, with the stirring rate controlled at 200 r / min throughout the process. After the reaction was completed, toluene was removed by vacuum distillation under 70 °C and 0.075 MPa negative pressure to obtain auxiliary agent B.

[0085] During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

[0086] The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

[0087] The reaction unit has a reaction temperature of 60°C, a reaction pressure of 0.3 MPa, and a residence time of 1 h.

[0088] The product separation unit employs a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 410℃, an operating pressure of 2kPa absolute pressure inside the column, and a bottom temperature of 345℃; it separates light and heavy fractions.

[0089] The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

[0090] The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 60℃, a pressure of 0.2MPa, and a residence time of 30min.

[0091] Table 1 shows the test results of sulfur content, kinematic viscosity, and calorific value of fuel oil in the specific implementation plan. Sulfur content (%) <![CDATA[Kinematic viscosity (mm 2 / s)]]> Calorific value (MJ / kg) Example 1 0.35 650 41.5 Example 2 0.28 590 42.3 Example 3 0.22 510 43.7 Example 4 0.16 460 44.2 Comparative Example 1 0.98 1430 28.9 Comparative Example 2 0.63 950 36.4 Comparative Example 3 0.51 830 37.8 The test data shows that the fuel oil produced by this device is superior to conventional process products in all three core indicators: sulfur content, kinematic viscosity, and calorific value. The key innovation is the compound additive system containing novel monomers, which effectively reduces the viscosity of heavy fractions, controls sulfur content, and increases calorific value. This allows the oil to simultaneously meet the high-performance requirements of low sulfur and environmental protection, smooth low-temperature combustion, and efficient combustion. The overall technical solution has significant advantages.

[0092] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Any person skilled in the art can make some modifications or alterations to the above-disclosed technical content to create equivalent embodiments without departing from the scope of the present invention. Any simple modifications, equivalent changes and alterations made to the above embodiments based on the technical essence of the present invention without departing from the scope of the present invention shall still fall within the scope of the present invention.

Claims

1. A low-sulfur, high-performance fuel oil production apparatus, characterized in that, It includes a raw material pretreatment unit, a reaction unit, a product separation unit, a viscosity reduction and modification unit, and a DCS automatic control unit; The raw material pretreatment unit is connected to four feed pipelines: low-sulfur modified residue oil, hydrotreated low-sulfur raffinate oil, additive A, and additive B. The auxiliary agent B is prepared by reacting dithiophosphoric acid, molybdenum trioxide, epoxy succinic acid polymer, 2,6-naphthalenedicarboxylic acid, and phosphorous acid.

2. The low-sulfur, high-performance fuel oil production apparatus according to claim 1, characterized in that: The amounts added to the four feed lines are as follows: 35-65 parts of low-sulfur modified residue oil, 15-30 parts of hydrotreated low-sulfur raffinate oil, 0.03-0.3 parts of additive A, and 0.02-0.2 parts of additive B.

3. The low-sulfur, high-performance fuel oil production apparatus according to claim 2, characterized in that: The additive A is composed of 20-40 parts of ethylene-vinyl acetate copolymer, 17-35 parts of polymethacrylate, and 15-25 parts of alkylnaphthalene.

4. The low-sulfur, high-performance fuel oil production apparatus according to claim 2, characterized in that: The preparation method of the aforementioned auxiliary agent B is as follows: By weight, 20-40 parts of dithiophosphoric acid, 7-14 parts of molybdenum trioxide, 0.5-2 parts of epoxy succinic acid polymer, 0.2-0.5 parts of 2,6-naphthalenedicarboxylic acid, 200-300 parts of anhydrous toluene, and 2-5 parts of phosphorous acid are mixed and then nitrogen is introduced to replace the air in the reactor 3-5 times. The temperature is raised to 85-100℃ and the reaction is carried out for 1-4 hours, with the stirring rate controlled at 200-350 r / min throughout the process. After the reaction is completed, toluene is removed by vacuum distillation under negative pressure conditions of 70-85℃ and 0.075-0.09 MPa to obtain auxiliary agent B.

5. A low-sulfur, high-performance fuel oil production apparatus according to claim 4, characterized in that: During the reaction process, the free acid value is detected by sampling, and the reaction is terminated when the acid value is ≤3mgKOH / g.

6. The low-sulfur, high-performance fuel oil production apparatus according to claim 1, characterized in that: The reaction unit is a pressure vessel lined with an austenitic-ferritic duplex stainless steel composite layer to achieve a low-temperature, mild reaction.

7. The low-sulfur, high-performance fuel oil production apparatus according to claim 1, characterized in that: The reaction unit has a reaction temperature of 60-80℃, a reaction pressure of 0.3-0.5MPa, and a residence time of 1-3h.

8. The low-sulfur, high-performance fuel oil production apparatus according to claim 1, characterized in that: The product separation unit adopts a vacuum deep-drawing technology, with a vacuum furnace outlet temperature of 410-430℃, an operating pressure of 2-3 kPa absolute pressure inside the column, and a bottom temperature of 345-365℃; it separates light and heavy fractions.

9. A low-sulfur, high-performance fuel oil production apparatus according to claim 7, characterized in that: The light fraction produced by the vacuum distillation can be used to produce Group III base oils after high-pressure hydroisomerization.

10. A low-sulfur, high-performance fuel oil production apparatus according to claim 7, characterized in that: The heavy fraction produced by the vacuum deep-drawing process enters the viscosity reduction and reforming unit. The viscosity reduction cracking reactor is a pressure vessel lined with an S22053 duplex stainless steel composite layer, with an operating temperature of 60-80℃, a pressure of 0.2-0.3MPa, and a residence time of 30-60min.

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