Marine fuel oil production device

Abstract

The utility model discloses a marine fuel oil production device which comprises a reaction tower, a heating furnace and a reduced pressure extraction tower, the reaction tower is connected with the heating furnace, the heating furnace is connected with the reduced pressure extraction tower, crude oil generates chemical reaction through the reaction tower, and a liquid mixture of wax oil and residual oil is separated out and enters the heating furnace; the system further comprises a visbreaking reaction tower and a flash tower, the visbreaking reaction tower is connected with the flash tower, the reduced pressure extraction tower is connected with the visbreaking reaction tower, the liquid residual oil is further subjected to a splitting reaction through the visbreaking reaction tower, and the liquid residual oil is further separated from the liquid mixture of the wax oil and the residual oil in the flash tower. The method has the advantages that the heavy oil is directly further processed to form the marine fuel oil, additional heavy oil production equipment does not need to be configured, the production cost is reduced, and the economic benefit is improved.

Description

Technical Field

[0001] This utility model relates to the chemical industry, and in particular to a marine fuel oil production apparatus. Background Technology

[0002] In the petrochemical industry, oil processing technology plays a crucial role in industry development and product quality. Early on, atmospheric distillation was a common method for oil separation, involving heating and separating oils under atmospheric pressure. However, this process has many drawbacks. Because it requires operation at relatively high temperatures, it not only consumes enormous amounts of energy, but the high-temperature environment also easily leads to reactions such as coking and polymerization in the oil, severely affecting oil quality and increasing production costs.

[0003] With technological advancements, vacuum distillation has emerged. Vacuum distillation separates oil products under negative pressure conditions. Its significant advantage lies in achieving oil separation at low temperatures, greatly reducing coking and polymer formation. Under the same conditions and where oil properties permit, vacuum distillation can save approximately 10% of energy compared to atmospheric distillation. This characteristic has led to its widespread application in the petrochemical industry. The light oil produced through vacuum distillation can serve as a high-quality raw material for downstream fine chemical plants, while the heavy oil is primarily used for the selective production of delayed coking feedstock or petroleum asphalt.

[0004] However, when heavy oil is used as feedstock in coking plants, market demand is not strong due to its relatively poor physical properties. While directly using heavy oil to produce petroleum asphalt results in products reaching end users, it fails to fully realize the refinery's economic potential, leading to a certain waste of resources. Refining heavy oil separately would increase production costs. Utility Model Content

[0005] The technical problem to be solved by this utility model is to provide a production device that can effectively utilize the heavy oil formed during vacuum distillation and further process the heavy oil into marine fuel oil, without the need for additional heavy oil production equipment, thereby reducing production costs and improving economic efficiency.

[0006] The technical solution adopted by this utility model to solve the above-mentioned technical problems is as follows: a marine fuel oil production device, including a reaction tower, a heating furnace and a vacuum extraction tower, wherein the reaction tower and the heating furnace are connected, and the heating furnace and the vacuum extraction tower are connected, wherein crude oil undergoes a chemical reaction in the reaction tower to separate a liquid mixture of wax oil and residue oil, which enters the heating furnace, and the heated liquid mixture of wax oil and residue oil is further separated into liquid residue oil in the vacuum extraction tower, wherein the device is characterized by further including a viscosity-reducing cracking tower and a flash distillation tower, wherein the viscosity-reducing cracking tower and the flash distillation tower are connected, and the vacuum extraction tower is connected to the viscosity-reducing cracking tower, wherein the liquid residue oil is further split in the viscosity-reducing cracking tower to form naphtha, first-line oil, wax oil and residue oil, and the sulfide substances are discharged through the flash distillation tower to form marine fuel oil containing naphtha, first-line oil, wax oil and residue oil.

[0007] A further preferred embodiment of this utility model is: the reaction tower and the vacuum extraction tower are connected, the crude oil produces a first gaseous mixture in the reaction tower, and a second gaseous mixture is produced in the vacuum extraction tower, and the first gaseous mixture and the second gaseous mixture are mixed together.

[0008] A further preferred embodiment of this utility model is that the first gaseous mixture is water, naphtha, and noncondensable gas, and the second gaseous mixture is naphtha and siphon oil.

[0009] A further preferred embodiment of this utility model is: it also includes a first centrifugal pump and a second centrifugal pump, the first centrifugal pump being disposed between the vacuum extraction tower and the viscosity reduction cracking tower reaction tower, and the second centrifugal pump being disposed at the discharge port of the flash tower.

[0010] A further preferred embodiment of this invention is: hydrogen sulfide is formed inside the flash tower, and the hydrogen sulfide is discharged as a gas inside the flash tower.

[0011] A further preferred embodiment of this utility model is: it also includes a static mixer, which is connected to the flash tower and the reaction tower, and the naphtha, extraction oil, wax oil and residue oil formed in the flash tower are discharged into the static mixer.

[0012] A further preferred embodiment of this utility model is as follows: a first level gauge is installed inside the vacuum extraction tower, a second level gauge is installed inside the flash evaporator, the vacuum extraction tower is connected to a first pressure gauge, and the flash evaporator is connected to a second pressure gauge.

[0013] A further preferred embodiment of this utility model is: a reaction tower top control valve is provided at the top of the reaction tower, and a pressure-reducing extraction tower top control valve is provided at the top of the pressure-reducing extraction tower.

[0014] A further preferred embodiment of this utility model is: a third centrifugal pump is connected to the inlet of the reaction tower, and a fourth centrifugal pump is provided between the reaction tower and the heating furnace.

[0015] This invention, by retaining the original vacuum extraction process, adds a viscosity-reducing cracking tower and a flash distillation tower. The viscosity-reducing cracking tower further breaks down the liquid residue oil, broadening the utilization pathways of the raw materials and producing a variety of components that meet the composition requirements of marine fuel oil. Heavy oil can be directly processed into marine fuel oil without the need for additional heavy oil production equipment, reducing production costs and improving economic efficiency. Attached Figure Description

[0016] Figure 1 This is a schematic diagram of the structure of this utility model;

[0017] Figure 2 This is a structural diagram of the existing design. Detailed Implementation

[0018] The present invention will be further described in detail below with reference to the accompanying drawings and embodiments.

[0019] like Figure 1 As shown, a marine fuel oil production unit includes a reaction tower 1, a heater 2, a vacuum extraction tower 3, a viscosity-reducing cracking tower reaction tower 4, and a flash tower 5. The reaction tower 1 is connected to the heater 2, the heater 2 is connected to the vacuum extraction tower 3, the vacuum extraction tower 3 is connected to the viscosity-reducing cracking tower reaction tower 4, and the viscosity-reducing cracking tower reaction tower 4 is connected to the flash tower 5. Crude oil first undergoes heat exchange to reach 300°C before entering the reaction tower 1. Inside the reaction tower 1, the crude oil undergoes a chemical reaction, causing water, naphtha, and non-condensable gases to be discharged in a gaseous state, while simultaneously forming a liquid mixture of wax oil and oil residue. The bottom pump of the reaction tower sends the dehydrated liquid mixture to the heater 2 for heating. The heater 2 heats the oil to 400°C before sending it to the vacuum extraction tower 3, which operates at a pressure of -100 kPa. In the vacuum extraction tower 3, the 400°C feed oil is separated into side stream light... Light oil, including naphtha and first-line oil, is directly extracted for the production of No. 5 fuel oil. Heavy oil includes residue oil. The heavy oil from the bottom of vacuum extraction tower 3 is pressurized by the bottom pump and sent to the viscosity-reducing cracking tower 4, which operates at 0.3 MPa and 360°C. The high-temperature modified residue oil flows upward in the viscosity-reducing cracking tower 4 and remains for 6 hours to undergo viscosity-reducing cracking. The modified residue oil at the top of the viscosity-reducing cracking tower 4 overflows to the flash tower 5, where it undergoes flash evaporation to separate hydrogen sulfide from the oil. The residue oil pump at the bottom of the flash tower 5 sends the modified residue oil, first-line oil, and wax oil to the static mixer 6 in the boundary area. The other mixing oil in the static mixer 6 is naphtha and first-line oil, which are thoroughly mixed and then sent to the tank area to produce qualified marine fuel oil. This invention makes full use of the high-temperature environment of the vacuum extraction tower, eliminating the need for separate heating during subsequent reaction processes and significantly reducing production costs.

[0020] This marine fuel oil production unit integrates the traditional atmospheric and vacuum distillation process with the viscosity-reducing cracking process, optimizes the process and heat exchange system, achieves complete system heat recovery and low energy consumption; it retains the original vacuum extraction process, and directly processes heavy oil to form marine fuel oil, which significantly reduces production costs.

[0021] Reactor 1 and vacuum extraction tower 3 are connected. Crude oil in reactor 1 produces a first gaseous mixture consisting of water, naphtha, and non-condensable gases. Vacuum extraction tower 3 produces a second gaseous mixture consisting of naphtha and extraction line oil. The first and second gaseous mixtures are then mixed, and the resulting gaseous mixture is further transported to static mixer 6 for further mixing, improving the stability and economy of the unit's operation.

[0022] This invention also includes a first centrifugal pump 7 and a second centrifugal pump 8. The first centrifugal pump 7 is located between the vacuum extraction tower 3 and the viscosity-reducing cracking tower 4, and the second centrifugal pump 8 is located at the outlet of the flash tower 5. The first centrifugal pump 7, located between the vacuum extraction tower 3 and the viscosity-reducing cracking tower 4, ensures that the liquid residue oil can be stably and efficiently transported to the viscosity-reducing cracking tower 4, maintaining the continuity of the reaction. The second centrifugal pump 8, located at the outlet of the flash tower 5, ensures that the marine fuel oil after flash treatment can be smoothly discharged, achieving continuous production, improving production efficiency, and ensuring stable operation of the unit.

[0023] Hydrogen sulfide is formed inside flash tower 5 and then discharged as a gas. Flash tower 5 effectively removes harmful sulfur components from marine fuel oil by discharging hydrogen sulfide in gaseous form. This reduces emissions of pollutants such as sulfur dioxide produced during the combustion of marine fuel oil, meeting environmental protection requirements, reducing atmospheric pollution, improving the quality of marine fuel oil, protecting ship equipment, and reducing corrosion and wear.

[0024] This invention also includes a static mixer 6, which connects the flash tower 5 and the reaction tower 1. The naphtha, first-line oil, wax oil, and residue oil formed in the flash tower 5 are discharged into the static mixer 6. The static mixer 6's connection to the flash tower 5 and the reaction tower 1 allows the naphtha, first-line oil, wax oil, and residue oil formed in the flash tower 5 to be further mixed with the substances in the reaction tower 1 after discharge. This helps to homogenize the product composition, improve product quality stability, optimize product performance, and meet the performance requirements of different marine engines for fuel oil.

[0025] A first level gauge 9 is installed inside the vacuum extraction tower 3, and a second level gauge 10 is installed inside the flash distillation tower 5. The vacuum extraction tower 3 is connected to a first pressure gauge 11, and the flash distillation tower 5 is connected to a second pressure gauge 12. The first level gauge 9 in the vacuum extraction tower 3 and the second level gauge 10 in the flash distillation tower 5 can monitor the liquid level in the towers in real time, facilitating timely adjustments to the operating parameters and preventing production accidents caused by excessively high or low liquid levels, thus ensuring the safe and stable operation of the unit. The first pressure gauge 11 and the second pressure gauge 12 monitor the pressure inside the two towers respectively, providing crucial data for controlling reaction conditions and optimizing the production process, ensuring that each tower operates under suitable pressure, and improving production efficiency and product quality.

[0026] A top control valve 13 is installed at the top of reaction tower 1, and a top control valve 14 is installed at the top of vacuum extraction tower 3. The top control valves 13 and 14 can flexibly control the discharge volume and rate of the gas from the top of the towers. By adjusting the valve opening, the pressure and material balance within the towers are optimized, ensuring the smooth progress of the reaction and separation processes in reaction tower 1 and vacuum extraction tower 3, and improving the operational flexibility and production stability of the unit.

[0027] A third centrifugal pump 15 is connected to the inlet of reaction tower 1, and a fourth centrifugal pump 16 is installed between reaction tower 1 and heater 2. The third centrifugal pump 15 at the inlet of reaction tower 1 ensures that crude oil can stably enter reaction tower 1, controls the feed rate and feed speed, and ensures the uniformity and stability of the reaction. The fourth centrifugal pump 16 between reaction tower 1 and heater 2 ensures that the liquid mixture of wax oil and residue oil after the reaction can smoothly enter heater 2, realizing continuous material transportation within the unit, improving production efficiency, and ensuring the smooth operation of the entire unit.

[0028] The above provides a detailed description of a leakage recovery system for a reciprocating pump provided by this utility model. Specific examples have been used to illustrate the principle and implementation of this utility model. The descriptions of the embodiments are merely for the purpose of helping to understand this utility model and its core ideas. It should be noted that those skilled in the art can make various improvements and modifications to this utility model without departing from its principles, and these improvements and modifications also fall within the protection scope of the claims of this utility model.

Claims

1. A marine fuel oil production apparatus, comprising a reaction tower, a heater, and a vacuum extraction tower, wherein the reaction tower and the heater are connected, and the heater and the vacuum extraction tower are connected, crude oil undergoes a chemical reaction in the reaction tower to separate a liquid mixture of wax oil and residue oil, which then enters the heater. The heated liquid mixture of wax oil and residue oil is further separated into liquid residue oil in the vacuum extraction tower, characterized in that... It also includes a viscosity-reducing cracking tower and a flash tower. The viscosity-reducing cracking tower and the flash tower are connected. A vacuum extraction tower is connected to the viscosity-reducing cracking tower. The liquid residue oil undergoes further cracking reaction in the viscosity-reducing cracking tower. Finally, the sulfurized substances are discharged through the flash tower to form marine fuel oil.

2. The marine fuel oil production apparatus according to claim 1, characterized in that... The reaction tower and the vacuum extraction tower are connected. The crude oil produces a first gaseous mixture in the reaction tower and a second gaseous mixture in the vacuum extraction tower. The first gaseous mixture and the second gaseous mixture are mixed together.

3. A marine fuel oil production apparatus according to claim 2, characterized in that... The first gaseous mixture is water, naphtha, and noncondensable gas, and the second gaseous mixture is naphtha and siphon oil.

4. A marine fuel oil production apparatus according to claim 1, characterized in that... It also includes a first centrifugal pump and a second centrifugal pump. The first centrifugal pump is located between the vacuum extraction tower and the viscosity reduction cracking tower, and the second centrifugal pump is located at the outlet of the flash tower.

5. A marine fuel oil production apparatus according to claim 1, characterized in that... Hydrogen sulfide is formed inside the flash tower, and then it is discharged as a gas inside the flash tower.

6. A marine fuel oil production apparatus according to claim 1, characterized in that... It also includes a static mixer, which connects the flash tower and the reaction tower. The naphtha, first-line oil, wax oil and residue oil formed in the flash tower are discharged into the static mixer.

7. A marine fuel oil production apparatus according to claim 1, characterized in that... The vacuum extraction tower is equipped with a first level gauge, the flash evaporator is equipped with a second level gauge, the vacuum extraction tower is connected to a first pressure gauge, and the flash evaporator is connected to a second pressure gauge.

8. A marine fuel oil production apparatus according to claim 1, characterized in that... The top of the reaction tower is equipped with a top control valve, and the top of the vacuum extraction tower is equipped with a top control valve.

9. A marine fuel oil production apparatus according to claim 1, characterized in that... A third centrifugal pump is connected to the inlet of the reaction tower, and a fourth centrifugal pump is installed between the reaction tower and the heating furnace.

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