CN113122330B - Method and system for preparing petroleum coke by catalyzing oil slurry and ethylene tar - Google Patents
Method and system for preparing petroleum coke by catalyzing oil slurry and ethylene tar Download PDFInfo
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- CN113122330B CN113122330B CN201911417742.3A CN201911417742A CN113122330B CN 113122330 B CN113122330 B CN 113122330B CN 201911417742 A CN201911417742 A CN 201911417742A CN 113122330 B CN113122330 B CN 113122330B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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Abstract
The invention discloses a method and a system for preparing petroleum coke by catalyzing oil slurry and ethylene tar, wherein the method comprises the following steps: removing solids from the catalytic slurry oil to obtain extracted oil and tail oil, carrying out hydrogenation treatment on the extracted oil, separating reaction products to obtain hydrogenated heavy distillate oil and ethylene tar, respectively heating the hydrogenated heavy distillate oil and the ethylene tar, then allowing the ethylene tar and the ethylene tar to enter a delayed coking device for reaction, stopping feeding of the ethylene tar when the reaction time reaches 1-50% of the whole reaction period, and separating the coking reaction products to obtain gas, light oil and heavy oil; and the light oil is mixed with hydrogenated heavy distillate oil after polymerization reaction, the mixture is heated and then enters a delayed coking device for reaction, and the heavy oil is recycled and mixed with catalytic slurry oil for solid removal treatment. The method can produce low-sulfur petroleum coke to the maximum extent by organically combining and processing the two raw materials, and the production device can stably run for a long period.
Description
Technical Field
The invention belongs to the technical field of petroleum processing, and particularly relates to a method for preparing low-sulfur petroleum coke.
Background
The aromatic carbon rate in catalytic slurry oil and ethylene tar is high, and when the catalytic slurry oil and the ethylene tar are used as raw materials to produce fuel oil, the obtained fuel oil has poor quality and is difficult to refine. However, a large amount of polycyclic aromatic hydrocarbons rich in the aromatic hydrocarbons are easy to form coke through thermal reaction, and the polycyclic aromatic hydrocarbons are high-quality raw materials for producing petroleum coke. With the production of the steel industry in China and the development of the industries such as new energy automobiles, the demand for low-sulfur petroleum coke is increasing day by day.
CN103789028A, CN104560152A, etc. disclose methods for producing needle coke by using catalytic slurry oil, and the needle coke belongs to special low sulfur petroleum coke. Compared with needle coke, the ordinary low-sulfur petroleum coke has low requirements on the properties of catalytic slurry oil and production process, i.e. most of the catalytic slurry oil can be treated to obtain the low-sulfur petroleum coke. CN104449799A and CN109609182A disclose a method for producing petroleum coke from ethylene tar, wherein the ethylene tar is distilled to obtain a light component, and the light component is heated to a reaction temperature by a heating furnace and then enters a coke tower to carry out a coking reaction. However, after the ethylene tar is subjected to distillation treatment, the residual oil at the temperature of more than 350 ℃ is usually solid or jelly, and is difficult to further process; and the extracted oil is heated to a temperature of more than 480 ℃ in the heating furnace to have violent reaction, so that the furnace tube is seriously coked, and the long-period operation of the device is not facilitated.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a method and a system for preparing petroleum coke by catalyzing oil slurry and ethylene tar, wherein the method and the system can be used for producing low-sulfur petroleum coke to the maximum extent and stably operating a production device for a long period by organically combining two raw materials.
The invention provides a method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, which comprises the following steps:
(1) removing solids from the catalytic slurry to obtain extraction oil and tail oil;
(2) mixing the extracted oil obtained in the step (1) with hydrogen, carrying out hydrogenation treatment in the presence of a hydrogenation catalyst, and separating reaction products to obtain gas, naphtha and hydrogenated heavy distillate oil;
(3) respectively heating the ethylene tar and the hydrogenated heavy distillate oil obtained in the step (2), then feeding the ethylene tar and the hydrogenated heavy distillate oil into a delayed coking device for reaction, stopping feeding the ethylene tar when the reaction time reaches 1-50%, preferably 10-40% of the whole reaction period, and separating the coking reaction product to obtain gas, light oil and heavy oil;
(4) polymerizing the light oil obtained in the step (3), mixing the polymerized light oil with the hydrogenated heavy distillate oil obtained in the step (2), heating the mixture, and reacting the mixture in a delayed coking device;
(5) and (4) recycling the heavy oil obtained in the step (3) to the step (1) to be mixed with catalytic slurry oil for solid removal treatment.
In the method for preparing petroleum coke from catalytic slurry oil and ethylene tar, the solid removal treatment in the step (1) can be one or more of filtration separation, centrifugal sedimentation and reduced pressure distillation treatment, and preferably reduced pressure distillation treatment. Further preferably, when vacuum distillation is used for the solid removal treatment, vacuum residue is added during the solid removal treatment, then a large amount of solid such as ash carried in catalytic slurry oil and coking heavy oil is removed through the vacuum residue, and after treatment, drawing oil and tail oil are obtained, and the drawing oil is discharged from the top of the tower. The 5 percent distillation temperature of the vacuum residue is 480-550 ℃, and preferably 500-540 ℃. The mass ratio of the catalytic slurry oil to the vacuum residue oil is 0.1: 1-10: 1, preferably 2: 1-5: 1.
In the method for preparing petroleum coke by using catalytic slurry oil and ethylene tar, the 95 percent distillation temperature of the drawn oil in the step (1) is 470-520 ℃, and the solid content of the drawn oil is not more than 0.01wt percent.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the hydrogenation reaction conditions in the step (2) are as follows: the reaction temperature is 310-470 ℃, preferably 325-420 ℃, the reaction pressure is 3-17 MPa, preferably 5-8 MPa, the volume ratio of hydrogen to oil is 300-2500, preferably 600-1600, wherein the volume ratio of hydrogen to oil is the volume ratio of hydrogen to extracted oil, and the liquid hourly space velocity is 0.1h-1～2.0h-1Preferably 0.3h-1～1.0h-1。
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the hydrogenation catalyst in the step (2) comprises a carrier and an active component, wherein the carrier is alumina or silicon-containing alumina, and the active component is an oxide of a metal in a VIB group and/or a VIII group, and specifically can be one or more of Mo, W, Co and Ni. The prior heavy oil hydrotreating catalyst in the field, such as FZC series hydrogenation catalyst developed by China petrochemical smoothing petrochemical research institute, can also be adopted. The hydrogenation catalyst can be used as a single catalyst or in combination of multiple catalyst grades.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the ethylene tar in the step (3) is full distillate oil which is not subjected to distillation treatment.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the delayed coking device in the step (3) comprises at least two heating furnaces, a fractionating system and two coke towers. Among the heating furnaces, at least one heating furnace is used for heating hydrogenated heavy distillate oil, and at least one heating furnace is used for heating ethylene tar. At least one of the coke drums is in a reaction stage and at least one of the coke drums is in a decoking stage.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the mass ratio of the hydrogenated heavy distillate oil to the ethylene tar in the step (3) is 1: 2-1: 0.01, preferably 1: 0.5-1: 0.1.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the reaction conditions of the delayed coking device in the step (3) are as follows: the outlet temperature of a heating furnace for heating the hydrogenated heavy distillate oil is 470-550 ℃, and preferably 480-510 ℃; the outlet temperature of the heating furnace for heating the ethylene tar is 200-420 ℃, and preferably 270-350 ℃; the top pressure of the coke tower is 0.01 MPa-2.5 MPa, preferably 0.5 MPa-1.0 MPa, and the coke tower can be operated at constant pressure or variable pressure, if the coke tower is operated at variable pressure, the pressure change rate is 0.01 MPa/h-50 MPa/h, preferably 0.2 MPa/h-5 MPa/h; the reaction period is 10-35 h, preferably 18-26 h.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, 95 percent distillation temperature of the light oil in the step (3) is 250-380 ℃, and preferably 270-310 DEG C
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the polymerization reaction conditions in the step (4) are as follows: the polymerization temperature is 350-550 ℃, preferably 380-450 ℃, the polymerization pressure is 0.01-5 MPa, preferably 1-3 MPa, and the retention time is 0.1-15 h, preferably 1-6 h.
In the method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the polymerization reactor in the step (4) is a fixed bed reactor, and a catalyst is filled in the polymerization reactor. The polymerization reactor comprises at least one feeding hole and two discharging holes, wherein the non-condensable gas generated by the polymerization reaction is discharged from the upper discharging hole, and the polymer is discharged from the lower discharging hole, mixed with the hydrogenation heavy distillate oil and returned to the delayed coking device. The catalyst takes one or more of kaolin, montmorillonite, alumina and silicon-containing alumina as a carrier, takes one or more of IVB group and/or VIB group metal oxides as an active component, and specifically can be at least one of Zr, W and Mo. The content of active components in the catalyst is 0.1-40 wt%, preferably 3-25 wt%. The shape of the catalyst can be one or more of a sphere, a cylinder, clover, raschig ring and the like.
The second aspect of the present invention provides a system for preparing petroleum coke by catalyzing oil slurry and ethylene tar, wherein the system comprises:
the solid removal reactor is used for receiving the catalytic slurry oil and obtaining the extraction oil and the tail oil after treatment;
the hydrogenation reaction unit is used for receiving hydrogen and the extracted oil from the solid removal reactor, and gas, naphtha and hydrogenated heavy distillate oil are obtained after reaction products are separated;
the device comprises a delayed coking device, a heavy hydrogenation distillate oil and ethylene tar are heated by respective heating furnaces and then enter a coking tower, the coking oil gas obtained after reaction enters a fractionation system, gas, naphtha, light oil and heavy oil are obtained after separation, and the heavy oil is circulated back to a solid removal reactor through a pipeline;
the polymerization reactor is used for receiving light oil from the coking fractionating tower, and the polymer obtained after the reaction is mixed with hydrogenated heavy distillate oil after the hydrogenation;
the delayed coking device comprises at least two heating furnaces, a fractionating system and two coke towers, wherein in the heating furnaces, at least one heating furnace is used for heating hydrogenated heavy distillate oil, at least one heating furnace is used for heating ethylene tar, at least one coke tower is in a reaction stage, at least one coke tower is in a decoking stage,
in the system for preparing petroleum coke by catalyzing slurry oil and ethylene tar, the hydrogenation reaction unit is provided with more than one hydrogenation reactor, and the hydrogenation reactors can be one or more of a fixed bed reactor, a fluidized bed reactor and a suspension bed reactor; preferably a fixed bed reactor.
In the system for preparing petroleum coke by catalyzing oil slurry and ethylene tar, the equipment adopted by the solid-removing reactor comprises any one or more of a filter, a centrifugal settler and a reduced pressure distillation tower, and the reduced pressure distillation tower is preferably adopted.
Compared with the prior art, the method and the system for preparing petroleum coke by catalyzing oil slurry and ethylene tar have the following advantages:
1. in the method for preparing the low-sulfur petroleum coke, in the first stage of the delayed coking reaction, the full-fraction ethylene tar is fed at low temperature, so that the ethylene tar is prevented from coking in a furnace tube, the retention time of the raw material in a low-temperature coke tower is prolonged, the coke yield is improved, and the problem that heavy components obtained after the ethylene tar is subjected to distillation treatment in the prior art cannot be treated is solved; in the second stage of reaction, the feeding of ethylene tar is stopped, and the hydrogenated high-temperature heavy distillate oil is fed separately, so that the reaction temperature in the coke tower is increased, the deep condensation of materials in the tower is promoted, and the soft coke is prevented from being produced. The method organically combines the catalytic oil slurry and the ethylene tar for treatment, not only makes full use of respective advantages of the two raw materials, but also can greatly improve the yield of the low-sulfur petroleum coke.
2. In the method for preparing the low-sulfur petroleum coke, because the sulfur in the whole reaction system is mainly enriched in the coke and the heavy oil, the method is favorable for relieving the severity of desulfurization on the extracted oil by hydrodesulfurization of the heavy oil, namely the extracted oil and the heavy oil can be subjected to hydrodesulfurization under relatively mild conditions, so that the requirements of coke products on sulfur content are met, the aromatic ring saturation rate can be effectively reduced, and the yield of the low-sulfur petroleum coke is improved.
3. In the method for preparing the low-sulfur petroleum coke, the light oil generated by the catalytic slurry oil through the delayed coking reaction belongs to low-sulfur high-aromatic oil, the stability is poor, and the post-treatment is difficult.
Drawings
FIG. 1 is a schematic diagram of a method for preparing low-sulfur petroleum coke by catalyzing oil slurry and ethylene tar according to the invention.
Detailed Description
The following examples are provided to further illustrate the process and effects of the present invention, but are not to be construed as limiting the scope of the present invention.
As can be seen from fig. 1, the present invention provides a method for preparing low-sulfur petroleum coke by catalyzing oil slurry and ethylene tar, which comprises the following steps: mixing the catalytic slurry oil 1 and the vacuum residue oil 2 at the bottom of a vacuum distillation tower 3, discharging tail oil 19 obtained after treatment from the bottom of the tower, feeding the obtained extracted oil 4 into a hydrogenation reaction unit 5, carrying out hydrogenation reaction with hydrogen, and separating reaction products to obtain gas, naphtha and hydrogenated heavy distillate oil; heating the hydrogenated heavy distillate oil 6 to a certain temperature by a heating furnace 7, and then feeding a material flow 8 into a coke tower 9A/B for reaction; after the ethylene tar 20 is heated to a certain temperature by a heating furnace 21, the material flow 22 is also sent to a coke tower 9A/B; the coking oil gas 10 passes through a coking fractionating tower 11 to separate gas 12, light oil 13 and heavy oil 14. Wherein, after the light oil 13 is treated by the polymerization reactor 17, the polymer 18 is mixed with the hydrogenated heavy distillate oil 6 for continuous reaction; the heavy oil 14 is recycled to the vacuum distillation column 3.
The properties of the catalytic slurry oil, ethylene tar and vacuum residue used in the following examples and comparative examples are shown in Table 1.
Example 1
Example 1 by adopting the process flow of the invention, catalytic slurry oil and vacuum residue oil are mixed at the bottom of a vacuum distillation tower in a mass ratio of 3:1, and 95% of the obtained extracted oil has a distillation temperature of 501 ℃; mixing the extracted oil with hydrogen and sending the mixture to a hydrogenation reaction unit to obtain hydrogenated heavy distillate oil; the hydrogenated heavy distillate oil and the ethylene tar are conveyed to a delayed coking device together according to the mass ratio of 1:0.15, the outlet temperature of a hydrogenated heavy distillate oil heating furnace is 493 ℃, the outlet temperature of an ethylene tar oil heating furnace is 298 ℃, when the feeding time reaches 30% of the reaction period, the ethylene tar oil is stopped feeding, the hydrogenated heavy distillate oil is independently fed into a delayed coking tower, and the delayed coking reaction adopts a constant-pressure operation process; separating gas, light oil and heavy oil from the generated coking oil gas by a fractionating tower, wherein the 95 percent distillation temperature of the light oil is 303 ℃; the heavy oil is sent to a vacuum distillation tower, the light oil is sent to a polymerization reactor, and the generated polymer is also returned to a delayed coking device. The specific reaction conditions are shown in Table 2. The results of the product distribution and coke sulfur content analyses are shown in Table 3.
Example 2
Example 2 adopts the process flow of the invention, and the difference from example 1 is that: the hydrogenated heavy distillate oil and the ethylene tar are conveyed to a delayed coking device together according to the mass ratio of 1:0.2, the outlet temperature of a hydrogenated heavy distillate oil heating furnace is 495 ℃, the outlet temperature of an ethylene tar heating furnace is 320 ℃, when the feeding time reaches 25% of the reaction period, the ethylene tar feeding is stopped, the hydrogenated heavy distillate oil is independently fed into a delayed coking tower, the delayed coking reaction adopts a pressure swing operation process, and when the feeding time reaches 50% of the reaction period, the pressure of the coke tower is relieved at the rate of 0.5 MPa/h. The specific reaction conditions are shown in Table 2. The results of the product distribution and coke sulfur content analysis are shown in Table 3.
Comparative example 1
In the comparative example 1, the catalytic slurry oil and the ethylene tar are treated by adopting the prior art to produce low-sulfur petroleum coke, namely, the catalytic slurry oil and the ethylene tar are mixed in advance and then heated by a heating furnace, the coking wax oil is directly recycled to a delayed coking device without being subjected to hydrotreating, and the coking light oil is discharged. Mixing the catalytic slurry oil and the vacuum residue oil at the bottom of the vacuum distillation tower in a mass ratio of 3:1 to obtain purified oil with 95 percent distillation temperature of 501 ℃; mixing the purified oil with hydrogen and sending the mixture to a hydrotreating system to obtain hydrogenated heavy distillate oil; mixing hydrogenated heavy distillate oil and ethylene tar according to the mass ratio of 1:0.13, heating the mixture to 495 ℃ through a heating furnace, and then sending the mixture to a coke tower, wherein the coke tower is operated at constant temperature and constant pressure; separating gas, light oil and heavy oil from the generated coking oil gas by a fractionating tower, wherein the 95 percent distillation temperature of the light oil is 348 ℃; heavy oil circulation vacuum distillation tower. The specific reaction conditions are shown in Table 2. The results of the product distribution and coke sulfur content analysis are shown in Table 3.
Comparative example 2
Comparative example 2 is essentially the same as comparative example 1 except for the specific reaction conditions, see table 2. The results of the product distribution and coke sulfur content analysis are shown in Table 3.
TABLE 1 Properties of the raw materials
TABLE 2 reaction conditions
TABLE 3 product distribution and Coke Sulfur content in hydrogenated heavy distillates and ethylene Tar
Claims (25)
1. A method for preparing petroleum coke by catalyzing oil slurry and ethylene tar, which comprises the following steps:
(1) removing solids from the catalytic slurry to obtain extraction oil and tail oil;
(2) mixing the extracted oil obtained in the step (1) with hydrogen, carrying out hydrogenation treatment in the presence of a hydrogenation catalyst, and separating reaction products to obtain gas, naphtha and hydrogenated heavy distillate oil;
(3) heating the ethylene tar and the hydrogenated heavy distillate oil obtained in the step (2) respectively, then feeding the heated ethylene tar and the hydrogenated heavy distillate oil into a delayed coking device for reaction, stopping feeding the ethylene tar when the reaction time reaches 1-50% of the whole reaction period, and separating the coking reaction products to obtain gas, light oil and heavy oil;
(4) polymerizing the light oil obtained in the step (3), mixing the polymerized light oil with the hydrogenated heavy distillate oil obtained in the step (2), heating the mixture, and reacting the mixture in a delayed coking device;
(5) and (4) recycling the heavy oil obtained in the step (3) to the step (1) to be mixed with catalytic slurry oil for solid removal treatment.
2. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: and (3) respectively heating the ethylene tar and the hydrogenated heavy distillate oil obtained in the step (2), then feeding the ethylene tar into a delayed coking device for reaction, stopping feeding the ethylene tar when the reaction time reaches 10-40% of the whole reaction period, and separating the coking reaction product to obtain gas, light oil and heavy oil.
3. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the solid removal treatment in the step (1) is one or more of filtration separation, centrifugal sedimentation and reduced pressure distillation treatment.
4. A process for the preparation of petroleum coke from catalytic slurry oil and ethylene tar according to claim 1 or 3, characterized in that: the solid removal treatment in the step (1) is reduced pressure distillation treatment.
5. The method of claim 4 for producing petroleum coke from ethylene tar and slurry oil by catalysis, wherein the petroleum coke comprises: when vacuum distillation is used for the solid removal treatment, vacuum residue is added during the solid removal treatment.
6. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 5, wherein: the 5% distillation temperature of the vacuum residue is 480-550 ℃, and the mass ratio of the catalytic slurry oil to the vacuum residue is 0.1: 1-10: 1.
7. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 5, wherein: the 5 percent distillation temperature of the vacuum residue is 500-540 ℃; the mass ratio of the catalytic slurry oil to the vacuum residue oil is 2: 1-5: 1.
8. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the 95 percent distillation temperature of the drawn oil in the step (1) is 470-520 ℃, and the solid content of the drawn oil is not more than 0.01 wt%.
9. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the hydrogenation reaction conditions in the step (2) are as follows:the reaction temperature is 310-470 ℃, the reaction pressure is 3-17 MPa, the volume ratio of hydrogen to oil is 300-2500, wherein the volume ratio of hydrogen to oil is the volume ratio of hydrogen to extracted oil, and the liquid hourly space velocity is 0.1h-1～2.0h-1。
10. The process for preparing petroleum coke from catalytic slurry oil and ethylene tar according to claim 1 or 9, wherein: the hydrogenation reaction conditions in the step (2) are as follows: the reaction temperature is 325-420 ℃, the reaction pressure is 5-8 MPa, the volume ratio of hydrogen to oil is 600-1600, wherein the volume ratio of hydrogen to oil is the volume ratio of hydrogen to extracted oil, and the liquid hourly space velocity is 0.3h-1～1.0h-1。
11. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the ethylene tar in the step (3) is full distillate which is not subjected to distillation treatment.
12. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the delayed coking unit in the step (3) comprises at least two heating furnaces, a fractionation system and two coke drums; among the heating furnaces, at least one heating furnace is used for heating hydrogenated heavy distillate oil, and at least one heating furnace is used for heating ethylene tar.
13. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the mass ratio of the hydrogenated heavy distillate oil to the ethylene tar in the step (3) is 1: 2-1: 0.01.
14. The process for preparing petroleum coke from catalytic slurry oil and ethylene tar as claimed in claim 1 or 13, wherein: the mass ratio of the hydrogenated heavy distillate oil to the ethylene tar in the step (3) is 1: 0.5-1: 0.1.
15. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the reaction conditions of the delayed coking unit in the step (3) are as follows: the outlet temperature of the heating furnace for heating the hydrogenated heavy distillate oil is 470-550 ℃, the outlet temperature of the heating furnace for heating the ethylene tar is 200-420 ℃, and the top pressure of the coke tower is 0.01-2.5 MPa.
16. The process for preparing petroleum coke from catalytic slurry oil and ethylene tar as claimed in claim 1 or 15, wherein: the reaction conditions of the delayed coking unit in the step (3) are as follows: the outlet temperature of a heating furnace for heating hydrogenated heavy distillate oil is 480-510 ℃; the outlet temperature of a heating furnace for heating the ethylene tar is 270-350 ℃; the top pressure of the coke tower is 0.5MPa to 1.0 MPa.
17. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: and (3) the 95 percent distillation temperature of the light oil in the step (3) is 250-380 ℃.
18. The process for preparing petroleum coke from catalytic slurry oil and ethylene tar as claimed in claim 1 or 17, wherein: and (3) the 95 percent distillation temperature of the light oil is 270-310 ℃.
19. The method for preparing petroleum coke by catalyzing oil slurry and ethylene tar according to claim 1, wherein: the polymerization reaction conditions in the step (4): the polymerization temperature is 350-550 ℃, the polymerization pressure is 0.01-5 MPa, and the retention time is 0.1-15 h.
20. The process for preparing petroleum coke from catalytic slurry oil and ethylene tar as claimed in claim 1 or 19, wherein: the polymerization reaction conditions in the step (4): the polymerization temperature is 380-450 ℃, the polymerization pressure is 1-3 MPa, and the retention time is 1-6 h.
21. A system for producing petroleum coke from catalytic slurry oil and ethylene tar, the system comprising:
the solid removal reactor is used for receiving the catalytic slurry oil and obtaining the extraction oil and the tail oil after treatment;
the hydrogenation reaction unit is used for receiving hydrogen and the extracted oil from the solid removal reactor, and gas, naphtha and hydrogenated heavy distillate oil are obtained after reaction products are separated;
the device comprises a delayed coking device, wherein hydrogenated heavy distillate oil and ethylene tar are heated by respective heating furnaces and then enter a coking tower, the coking oil gas obtained after reaction enters a fractionation system, gas, naphtha, light oil and heavy oil are obtained after separation, and the heavy oil is circulated back to a solid removal reactor through a pipeline;
the polymerization reactor is used for receiving light oil from the coking fractionating tower, and the polymer obtained after the reaction is mixed with hydrogenated heavy distillate oil after the hydrogenation;
the delayed coking device comprises at least two heating furnaces, a fractionating system and two coke drums, wherein in the heating furnaces, at least one heating furnace is used for heating hydrogenated heavy distillate oil, at least one heating furnace is used for heating ethylene tar, at least one coke drum is in a reaction stage, and at least one coke drum is in a decoking stage.
22. The system for producing petroleum coke from catalytic slurry oil and ethylene tar as set forth in claim 21, wherein: the hydrogenation reaction unit is provided with more than one hydrogenation reactor, and the hydrogenation reactors are one or more of fixed bed reactors, fluidized bed reactors and suspension bed reactors.
23. The system for producing petroleum coke from catalytic slurry oil and ethylene tar as claimed in claim 21 or 22, wherein: the hydrogenation reaction unit is provided with more than one hydrogenation reactor, and the hydrogenation reactors are fixed bed reactors.
24. The system for producing petroleum coke from catalytic slurry oil and ethylene tar as set forth in claim 21, wherein: the equipment adopted by the solid removal reactor comprises any one or more of a filter, a centrifugal settler and a reduced pressure distillation tower.
25. The system for producing petroleum coke from catalytic slurry oil and ethylene tar as claimed in claim 21 or 24, wherein: the solid removal reactor adopts a reduced pressure distillation tower.
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| CN102260529A (en) * | 2010-05-27 | 2011-11-30 | 中国石油化工股份有限公司 | Combined method for processing inferior heavy oil |
| CN103805248A (en) * | 2012-11-08 | 2014-05-21 | 中国石油化工股份有限公司 | Method for producing clean fuel oil from ethylene tar |
| CN107987880A (en) * | 2016-10-26 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of method and apparatus for preparing needle-shape coke raw material |
| CN109929592A (en) * | 2017-12-15 | 2019-06-25 | 中国石油化工股份有限公司 | A kind for the treatment of process and system of ethylene bottom oil |
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2019
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260529A (en) * | 2010-05-27 | 2011-11-30 | 中国石油化工股份有限公司 | Combined method for processing inferior heavy oil |
| CN103805248A (en) * | 2012-11-08 | 2014-05-21 | 中国石油化工股份有限公司 | Method for producing clean fuel oil from ethylene tar |
| CN107987880A (en) * | 2016-10-26 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of method and apparatus for preparing needle-shape coke raw material |
| CN109929592A (en) * | 2017-12-15 | 2019-06-25 | 中国石油化工股份有限公司 | A kind for the treatment of process and system of ethylene bottom oil |
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