Slurry bed residual oil hydrocracking light dirty oil recycling method
By using the light-fouling oil refining method in the residual oil hydrocracking slurry bed device, fractionating and cooling the light-fouling oil components, the problem of light-fouling oil treatment is solved, the utilization rate and yield of oil are improved, and the treatment cost and environmental pollution are reduced.
Patent Information
- Application Number
- CN202510217684.9
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-02-26
- Publication Date
- 2025-04-11
AI Technical Summary
If the light dirty oil produced by the hydrocracking slurry bed device of residual oil cannot be processed and utilized in a timely and effective manner, it will cause waste of resources and environmental pollution. Traditional treatment methods have safety hazards and high treatment costs.
A slurry bed residual oil hydrocracking light-fouling oil refining method is adopted. By pumping the light-fouling oil into the fractionation feed buffer tank, the acidic water is removed, and then the light-fouling oil with the acidic water is pumped into the atmospheric fractionation tower for fractionation, the temperature and pressure are controlled to cut the light-fouling oil components, and finally the different fractions are cooled and stored.
Effectively reduce the frequency of light-fouling oil delivery, reduce the treatment pressure in the tank area, improve the utilization and yield of oil products, reduce energy consumption, and have good economic and environmental benefits.
Smart Images
Figure CN119799361A_ABST
Abstract
Description
Technical Field
[0001] The invention relates to the technical field of petrochemical industry, in particular to a slurry bed residue oil hydrocracking light dirty oil recycling method. Background Art
[0002] During the production process of the residue oil hydrocracking slurry bed, a large amount of light dirty oil will be generated. The sources of these light dirty oils are: the waste oil generated during the isolation, maintenance, and commissioning of the pumps or equipment in the device is discharged to the light dirty oil tank; during normal production, the waste oil generated by the laboratory sampling operation needs to be replaced and discharged to the light dirty oil tank; in summer or at high temperature, when the cooling effect of the air cooler is not good, the air cooler needs to be purged and replaced, and the waste oil generated is discharged to the light dirty oil tank; the waste lubricating oil generated when the compressor or large machine pump is running is collected together and poured into the light dirty oil tank; the waste oil generated when the compressor vent pipeline is condensed is discharged to the light dirty oil tank; the water-containing dirty oil separated by the acid water separation device; the light hydrocarbons generated when the circulating hydrogen desulfurization, liquefied gas desulfurization, dry gas desulfurization and other systems skimming.
[0003] It can be seen that the residue hydrocracking slurry bed unit will produce a large amount of light dirty oil. If these light dirty oils cannot be treated and utilized in a timely and effective manner, it will not only cause a waste of resources, but also pollute the environment. The traditional treatment method is to send them to the tank area device and then conduct subsequent centralized treatment, resulting in a large amount of light dirty oil accumulation, which not only poses a great safety hazard, but also has high subsequent treatment costs and a large treatment volume. Summary of the invention
[0004] The purpose of the present invention is to overcome the shortcomings of the prior art and propose a slurry bed residue oil hydrocracking light dirty oil refining method, which can effectively reduce the frequency of light dirty oil delivery, reduce the pressure and load of light dirty oil processing in the tank area, and improve the utilization rate and oil yield of oil products.
[0005] The technical solution adopted by the present invention to solve the technical problem is:
[0006] A slurry bed residue oil hydrocracking light dirty oil recycling method, comprising:
[0007] The light dirty oil in the light dirty oil tank is pumped into the fractionation feed buffer tank, the acid water carried by the light dirty oil is removed from the fractionation feed buffer tank, and then the light dirty oil with the acid water removed is pumped into the atmospheric pressure fractionation tower;
[0008] Control the temperature and pressure at the top and bottom of the atmospheric distillation tower, control the top temperature of the atmospheric distillation tower to 120-152°C, the top pressure to 0.15-0.3MPa, control the bottom temperature of the atmospheric distillation tower 3 to 210-280°C, the bottom pressure to 0.25-0.5MPa, and cut the fraction of the light dirty oil component;
[0009] After cutting, different fractions are obtained, including naphtha fraction, diesel fraction and wax oil fraction, etc.
[0010] The different fractions after separation are cooled and transported to different storage tanks for collection and storage.
[0011] Furthermore, the different fractions after separation are cooled, the naphtha fraction is cooled to 30-60°C by a naphtha cooler, the diesel fraction is cooled to 40-80°C by a diesel water cooler and a diesel air cooler, and the wax oil fraction is controlled at 85-95°C by a wax oil air cooler.
[0012] Furthermore, the light dirty oil tank is arranged underground or above ground.
[0013] Furthermore, the light-dirty oil tank is equipped with a liquid level detection system, a pressure detection system and a temperature detection system, which are used to detect the liquid level, internal pressure and temperature of the light-dirty oil tank respectively.
[0014] Furthermore, the liquid level inside the light dirty oil tank is controlled at 20% to 80% of the internal volume of the light dirty oil tank, the pressure is controlled at 10KPa to 70KPa, and the temperature does not exceed 90°C.
[0015] Furthermore, the outlet flow rate of the light oil tank is controlled at 10 t / h to 20 t / h.
[0016] The present invention also provides another technical solution:
[0017] A slurry bed residue oil hydrocracking light dirty oil recycling device comprises a light dirty oil tank, a fractionation feed buffer tank, an atmospheric pressure fractionation tower and an acidic water tank; the light dirty oil tank is connected to the fractionation feed buffer tank through a light dirty oil recycling pipeline, and a light dirty oil pump is arranged on the light dirty oil recycling pipeline; the bottom of the fractionation feed buffer tank is connected to the atmospheric pressure fractionation tower and the acidic water tank. The light dirty oil separated from the acidic water is transported to the atmospheric pressure fractionation tower for fractionation.
[0018] Furthermore, a feed pump is provided on the pipeline between the fractionation feed buffer tank and the atmospheric pressure fractionation tower, and the medium and light waste oil in the fractionation feed buffer tower is pumped into the atmospheric pressure fractionation tower by the feed pump.
[0019] Furthermore, one end of the light oil recycling pipeline is connected to the distillation feed buffer tank, and the other end is connected to the light oil export pipeline. One end of the light oil export pipeline is connected to the light oil tank, and the other end is connected to the export device. The export device transports the light oil in the light oil tank to the export device through the light oil export pipeline, and the export device transports it to a designated location.
[0020] Technical effects of the present invention:
[0021] Compared with the prior art, the slurry bed residue oil hydrocracking light dirty oil refining method of the present invention adopts separation technology to effectively separate high-quality products, improve the utilization rate of light dirty oil, the yield of oil products and the added value of products, reduce the processing pressure and load of light dirty oil tanks on light dirty oil, save energy, reduce energy consumption, and reduce the frequency of sending light dirty oil. The present invention is easy to operate, has low operating cost, and has good economic and environmental benefits. BRIEF DESCRIPTION OF THE DRAWINGS
[0022] Figure 1 It is a schematic structural diagram of the slurry bed residue oil hydrocracking light dirty oil recycling device of the present invention.
[0023] In the figure, 1. light dirty oil tank; 2. distillation feed buffer tank; 3. atmospheric pressure fractionation tower; 4. acid water tank; 5. light dirty oil refining pipeline; 6. light dirty oil pump; 7. feed pump; 8. light dirty oil delivery pipeline; 9. top reflux pump; 10. middle reflux pump; 11. bottom discharge pump; 12. flow meter; 13. delivery device; 14. naphtha cooler; 15. diesel water cooler; 16. diesel air cooler; 17. wax oil air cooler; 18. transportation pipeline; 19. reflux tank; 20. reflux pipe. DETAILED DESCRIPTION
[0024] In order to make the purpose, technical solution and advantages of the embodiments of the present invention more clear, the technical solution in the embodiments of the present invention is clearly and completely described below in conjunction with the accompanying drawings.
[0025] Embodiment 1:
[0026] The present embodiment relates to a slurry bed residue oil hydrocracking light dirty oil recycling method, which is realized based on a slurry bed residue oil hydrocracking light dirty oil recycling device.
[0027] like Figure 1 As shown, the slurry bed residue oil hydrocracking light dirty oil recycling device comprises a light dirty oil tank 1, a fractionation feed buffer tank 2, an atmospheric pressure fractionation tower 3 and an acidic water tank 4; the light dirty oil tank 1 is connected to the fractionation feed buffer tank 2 through a light dirty oil recycling pipeline 5, and a light dirty oil pump 6 is arranged on the light dirty oil recycling pipeline 5; the bottom of the fractionation feed buffer tank 2 is connected to the atmospheric pressure fractionation tower 3 and the acidic water tank 4. The light dirty oil from which the acidic water is removed is transported to the atmospheric pressure fractionation tower 3 for fractionation.
[0028] The top, middle section and bottom of the atmospheric distillation tower 3 are connected to a naphtha output pipe, a diesel output pipe and a wax oil output pipe respectively. The naphtha output pipe is provided with a reflux tank 19, a top reflux pump 9 and a naphtha cooler 14. The diesel output pipe is provided with a middle section reflux pump 10, a diesel water cooler 15 and a diesel air cooler 16. The wax oil output pipe is provided with a bottom discharge pump 11 and a wax oil air cooler 17. A reflux pipe 20 is provided between the naphtha output pipe, the diesel output pipe and the atmospheric distillation tower 3.
[0029] The pipeline between the fractionation feed buffer tank 2 and the atmospheric pressure fractionation tower 3 is provided with a feed pump 7, and the medium light oil pump 6 of the fractionation feed buffer tower is pumped into the atmospheric pressure fractionation tower 3 by the feed pump 7. One end of the light oil recycling pipeline 5 is connected to the fractionation feed buffer tank 2, and the other end is connected to the light oil export pipeline 8. One end of the light oil export pipeline 8 is connected to the light oil tank 1, and the other end is connected to the export device 13. The export device 13 transports the light oil in the light oil tank 1 to the export device 13 through the light oil export pipeline 8, and the export device 13 transports the light oil to the designated location.
[0030] In this embodiment, the light dirty oil tank 1 is set underground. The light dirty oil tank 1 is equipped with a liquid level detection system, a pressure detection system and a temperature detection system, which are respectively used to detect the liquid level height, internal pressure and temperature of the light dirty oil tank 1. A flow meter 12 is set on the light dirty oil recycling pipeline 5 to measure the light dirty oil transportation flow rate. The slurry bed residue oil hydrocracking light dirty oil recycling device also includes a control system, which is connected to the liquid level detection system, the pressure detection system, the temperature detection system and the flow meter 12 to achieve automatic control.
[0031] The slurry bed residue oil hydrocracking light dirty oil recycling method comprises:
[0032] The light dirty oil in the light dirty oil tank 1 is pumped 6 into the fractionation feed buffer tank 2, and the outlet flow of the light dirty oil tank 1 is controlled at 10t / h-20t / h. The acid water carried by the light dirty oil is removed from the fractionation feed buffer tank 2, and then the light dirty oil pump 6 with the acid water removed is sent to the atmospheric pressure fractionation tower 3;
[0033] Control the temperature and pressure at the top and bottom of the atmospheric distillation tower 3, control the top temperature of the atmospheric distillation tower 3 to 120-152°C, the top pressure to 0.15-0.3MPa, control the bottom temperature of the atmospheric distillation tower 3 to 210-280°C, and the bottom pressure to 0.25-0.5MPa. The setting of the temperature and pressure can form a reasonable temperature gradient and pressure gradient from the bottom to the top in the atmospheric distillation tower 3, separate the various components of the light dirty oil, and set the top reflux pump 9, the middle section reflux pump 10 and the bottom discharge pump 11 to accurately control the temperature of the atmospheric distillation tower 3, and cut and purify the fraction of the light dirty oil component;
[0034] After cutting, different fractions are obtained, including naphtha fraction, diesel fraction and wax oil fraction, etc.
[0035] The different fractions after separation are cooled, the naphtha fraction is cooled to 30-60°C by the naphtha cooler 14, the diesel fraction is cooled to 40-80°C by the diesel water cooler 15 and the diesel air cooler 16, and the wax oil fraction is controlled at 85-95°C by the wax oil air cooler 17, and are respectively transported to different storage tanks for collection and storage.
[0036] Other feed materials can enter the light dirty oil tank 1 through the delivery pipeline 18, and the light dirty oil and other feed materials are mixed in a certain ratio and pumped into the fractionation feed buffer tank 2. Specifically, the light dirty oil and the cold high-fraction oil produced by the slurry bed reaction system are mixed in a ratio of (1-5): (10-80), at which the wax oil component in the light dirty oil can be completely dissolved in the cold high-fraction oil, and the temperature of the fractionation feed buffer tank 2 is controlled to be 35-55°C, and the top pressure of the fractionation feed buffer tank 2 is 0.15-0.25MPa.
[0037] The liquid level inside the light dirty oil tank 1 is controlled at 20% to 80% of the internal volume of the light dirty oil tank 1, the pressure is controlled at 10KPa to 70KPa, and the temperature does not exceed 90°C. When the liquid level inside the light dirty oil tank 1 is high, the light dirty oil pump 6 is started by the control system to send the light dirty oil to the fractionation feed buffer tank 2. When the liquid level is below 30%, the pump should be stopped immediately to prevent the light dirty oil pump 6 from being emptied. When the temperature of the light dirty oil tank 1 exceeds 90°C, it is strictly forbidden to start the pump to prevent the pump from being emptied due to vaporization of the medium at the inlet of the light dirty oil pump 6.
[0038] The light dirty oil from which the acidic water is removed in the present invention passes through the top reflux pump 9, the middle section reflux pump 10 and the bottom discharge pump 11 of the atmospheric distillation tower 3, and the oil products of different fractions are separated. For example, the top of the atmospheric distillation tower 3 produces naphtha, the middle section of the atmospheric distillation tower 3 produces diesel, and the bottom of the atmospheric distillation tower 3 produces wax oil. The fractions of the light dirty oil components are cut, the utilization rate of the light dirty oil and the yield of the oil products are improved, and the added value of the products is increased. Finally, after the oil products are cooled down, they are respectively sent to qualified product storage tanks for collection and storage, which reduces the frequency of sending the light dirty oil.
[0039] The above-mentioned specific implementation modes are only specific cases of the present invention. The patent protection scope of the present invention includes but is not limited to the above-mentioned specific implementation modes. Any appropriate changes or modifications made thereto by any ordinary technician in the technical field in accordance with the claims of the present invention shall fall within the patent protection scope of the present invention.
Claims
1. A slurry bed residue oil hydrocracking light dirty oil refining method, characterized in that: include: The light dirty oil in the light dirty oil tank is pumped into the fractionation feed buffer tank, the acid water carried by the light dirty oil is removed from the fractionation feed buffer tank, and then the light dirty oil with the acid water removed is pumped into the atmospheric pressure fractionation tower; Control the temperature and pressure at the top and bottom of the atmospheric distillation tower, control the top temperature of the atmospheric distillation tower to 120-152°C, the top pressure to 0.15-0.3MPa, control the bottom temperature of the atmospheric distillation tower 3 to 210-280°C, the bottom pressure to 0.25-0.5MPa, and cut the fraction of the light dirty oil component; After cutting, different fractions are obtained; The different fractions after separation are cooled and transported to different storage tanks for collection and storage.
2. The slurry bed residue hydrocracking light dirty oil refining method according to claim 1, characterized in that: The different fractions after separation are cooled, the naphtha fraction is cooled to 30-60°C through a naphtha cooler, the diesel fraction is cooled to 40-80°C through a diesel water cooler and a diesel air cooler, and the wax oil fraction is controlled at 85-95°C through a wax oil air cooler.
3. The slurry bed residue hydrocracking light dirty oil refining method according to claim 1, characterized in that: The light dirty oil tank is arranged underground or above ground.
4. The slurry bed residue hydrocracking light dirty oil refining method according to claim 1, characterized in that: The light-dirty oil tank is equipped with a liquid level detection system, a pressure detection system and a temperature detection system, which are used to detect the liquid level height, internal pressure and temperature of the light-dirty oil tank respectively.
5. The slurry bed residue hydrocracking light dirty oil refining method according to claim 1, characterized in that: The liquid level inside the light dirty oil tank is controlled at 20% to 80% of the internal volume of the light dirty oil tank, the pressure is controlled at 10KPa to 70KPa, and the temperature does not exceed 90°C.
6. The slurry bed residue hydrocracking light dirty oil refining method according to claim 1, characterized in that: The outlet flow rate of the light oil tank is controlled at 10t / h to 20t / h.
7. A slurry bed residue oil hydrocracking light dirty oil recycling device, used to implement the slurry bed residue oil hydrocracking light dirty oil recycling method according to any one of claims 1 to 6, characterized in that: The device comprises a light-dirty oil tank, a fractionation feed buffer tank, a normal-pressure fractionation tower and an acidic water tank; the light-dirty oil tank is connected to the fractionation feed buffer tank via a light-dirty oil recycling pipeline, and a light-dirty oil pump is arranged on the light-dirty oil recycling pipeline; the bottom of the fractionation feed buffer tank is connected to the normal-pressure fractionation tower and the acidic water tank.
8. The slurry bed residue oil hydrocracking light dirty oil recycling device according to claim 7, characterized in that: A feed pump is arranged on the pipeline between the fractionation feed buffer tank and the atmospheric pressure fractionation tower.
9. The slurry bed residue oil hydrocracking light dirty oil recycling device according to claim 7, characterized in that: One end of the light oil recycling pipeline is connected to the distillation feed buffer tank, and the other end is connected to the light oil export pipeline. One end of the light oil export pipeline is connected to the light oil tank, and the other end is connected to the export device.