Modularized ethylene tar processing device and processing method

Abstract

The top of a first rectifying tower is connected with a first heat exchange unit, the bottom of the first rectifying tower is connected with a second preheater, the first heat exchange unit is connected with a first return tank, the first return tank is connected with the top of the first rectifying tower, and the second preheater is connected with a second rectifying tower. The top of the second rectifying tower is connected with the second heat exchange unit, the bottom of the second rectifying tower is connected with the first reaction kettle, the second heat exchange unit is connected with the second reflux tank, the second reflux tank is connected with the top of the second rectifying tower and the light oil receiving tank, and the upper ends of the first reaction kettle and the second reaction kettle are connected with the cooling unit; the first rectifying tower is respectively connected with the first reaction kettle and the second reaction kettle, the lower end of the second reaction kettle is connected with the short-path molecular distiller, and the short-path molecular distiller is connected with the heavy component receiving tank and the light component receiving tank. By adopting a modular structural design, the process flow can be adjusted as required, and meanwhile, the comprehensive utilization rate of ethylene tar is increased.

Description

Technical Field

[0001] This invention relates to the field of ethylene tar processing technology, and specifically to a modular ethylene tar processing apparatus and processing method. Background Technology

[0002] Ethylene tar is a product of the high-temperature condensation of ethylene cracking feedstock during the cracking process. Its initial boiling point is generally between 180-240℃, and its final boiling point is generally between 400-500℃. Ethylene tar is mainly composed of four components: saturated components, aromatic components, gums, and asphaltenes. It has low sulfur and nitrogen content and does not contain metallic impurities.

[0003] Currently, how to effectively reduce emissions and increase efficiency, extend the processing routes of petroleum products, and improve the added value of petroleum products have become urgent problems to be solved.

[0004] To increase the added value of ethylene tar, various comprehensive utilization methods have been developed, such as catalytic hydrogenation to produce gasoline and diesel products, and solvent deasphalting to use the heavy components as general-purpose carbon fiber raw materials and lithium battery anode coating materials. However, some of these methods are immature, energy-intensive, require multiple reactors and towers for switching, produce anode coating materials with low coking values, and the light components can only be used as marine fuel oil. Furthermore, the comprehensive utilization rate of ethylene tar is low, and it is difficult to achieve multi-product co-production in the same unit, making it difficult to flexibly adjust the process flow. Summary of the Invention

[0005] The purpose of this invention is to provide a modular ethylene tar processing apparatus and method, which at least solves one of the technical problems existing in the prior art.

[0006] To solve the above-mentioned technical problems, the present invention adopts the following technical solution:

[0007] This invention discloses a modular ethylene tar processing apparatus, comprising a first preheater, a first distillation column, a first heat exchange unit, a first reflux tank, a second preheater, a second distillation column, a second heat exchange unit, a second reflux tank, a light oil receiving tank, a first reactor, a second reactor, a cooling unit, a short-path molecular distillation apparatus, a heavy component receiving tank, a light component receiving tank, granulation equipment, a distillation column vacuum pump, a reactor vacuum pump, and a short-path molecular vacuum pump. The first preheater is connected to the first distillation column; the top of the first distillation column is connected to the first heat exchange unit, and the bottom is connected to the second preheater. The first heat exchange unit is connected to the first reflux tank, and the first reflux tank is connected to the top of the first distillation column. The first reflux tank transports a first product to a finished product tank area via a pipeline as feedstock for catalytic hydrodiesel. The second preheater is connected to the second distillation column; the top of the second distillation column is connected to the second heat exchange unit, and the bottom is connected to the first reactor. The second heat exchange unit is connected to the second reflux tank, and the second reflux tank is connected to both the top of the second distillation column and the light oil receiving tank. The light oil receiving tank transports the second product to the finished product tank area via pipeline as marine fuel oil. The distillation column vacuum pump is used to evacuate the first and second distillation columns. The first and second reaction vessels are connected, and the upper ends of both are connected to the cooling unit, while their lower ends are connected to the granulation equipment. The cooling unit transports the third product to the finished product tank area via pipeline as marine fuel oil. The reaction vessel vacuum pump is used to evacuate the first and second reaction vessels. The first distillation column is connected to the first and second reaction vessels via pipeline. The lower end of the second reaction vessel is connected to the short-path molecular still. The short-path molecular still is connected to the heavy component receiving tank and the light component receiving tank. The heavy component receiving tank is connected to the granulation equipment. The light component receiving tank transports the fourth product to the finished product tank area via pipeline as a rubber plasticizer. The short-path molecular vacuum pump is used to evacuate the short-path molecular still. A cold trap is provided between the short-path molecular still and the short-path molecular vacuum pump.

[0008] This technology employs a modular structural unit design, where the first and second distillation columns, the first and second reaction vessels are interconnected via cross-lines. This allows for combinations of different processes, such as one column and one reactor, two columns and one reactor, two columns and two reactors, and one column and two reactors. These combinations can meet users' requirements for different coated asphalts. Process adjustments are simple, and the process flow can be adjusted as needed, improving production flexibility. Furthermore, the multi-reaction unit setup can produce a variety of products, including hydrotreated diesel feedstock, marine fuel oil, rubber plasticizers, and 100℃-290℃ negative electrode coated asphalt. This enables comprehensive utilization of ethylene tar, resulting in a diverse range of products and significantly enhancing the comprehensive utilization value of ethylene tar. This technical solution continuously separates and removes light components from the product, improving the product composition distribution. Even with the same softening point, the resulting product also exhibits a higher asphalt coking value.

[0009] Furthermore, to more fully utilize ethylene tar, the system also includes a precision distillation column, a third heat exchange unit, a third reflux tank, a fourth heat exchange unit, a reboiler, and a vacuum pump unit. The first reflux tank is connected to the precision distillation column via a pipeline. The top of the precision distillation column is connected to the third heat exchange unit, and the bottom is connected to both the fourth heat exchange unit and the reboiler. The third reflux tank is connected to both the third heat exchange unit and the top of the precision distillation column. The third reflux tank transports the fifth product to the finished product tank area as a C9 product via a pipeline. The fourth heat exchange unit transports the sixth product to the finished product tank area as a feedstock for hydrotreated diesel via a pipeline. The reboiler refluxes the bottom product of the precision distillation column back into the precision distillation column via a pipeline. The vacuum pump unit is used to evacuate the precision distillation column.

[0010] Furthermore, in order to better achieve the heat exchange effect on the top product of the precision distillation column, the third heat exchange unit includes a B condenser and a B aftercooler. The top of the precision distillation column is connected to the B condenser and the B aftercooler in sequence, and the B aftercooler is connected to the third reflux tank.

[0011] Furthermore, a first pump is connected to the bottom of the first distillation column, and the first pump is connected to a first reboiler and a first evaporator through pipes. The first reboiler and the first evaporator are connected to the upper part of the stripping section tray in the first distillation column through pipes. A second pump is connected to the bottom of the second distillation column, and the second pump is connected to a second reboiler and a second evaporator through pipes. The second reboiler and the second evaporator are connected to the upper part of the stripping section tray in the second distillation column through pipes.

[0012] At this point, due to the setup of the first reboiler and the first evaporator, the unvaporized heavy components enter the bottom of the first distillation column, are pumped to the first reboiler and the first evaporator by the first pump, and then enter the upper part of the stripping section trays of the first distillation column. The kinetic energy of the rising gas phase propels the heavy components forward, causing the gas and liquid phases to flow in the same direction on the trays, reducing the liquid level difference, increasing the gas flow velocity and the number of distribution points, increasing the liquid surface area, and increasing the probability of light components escaping. After the light components escape, the heavy components can accumulate in the bottom of the column, increasing the softening point of the asphalt in the bottom of the column, thus narrowing the distribution of asphalt components. This allows for a narrower distribution of asphalt components with the same softening point, resulting in more uniform coating during asphalt use and reducing the difficulty of treating tail gas caused by asphalt volatiles. The second reboiler and the second evaporator are set up on the same principle.

[0013] Furthermore, in order to better achieve the heat exchange effect on the top product of the first distillation column, the first heat exchange unit includes an A preheater and an A condenser, which are sequentially connected between the top of the first distillation column and the first reflux tank.

[0014] Furthermore, in order to better achieve the heat exchange effect on the top product of the second distillation column, the second heat exchange unit includes a B preheater and a B cooler, which are connected in sequence between the top of the second distillation column and the second reflux tank.

[0015] Furthermore, both the first and second reaction vessels are slender with a length-to-diameter ratio of 1:2 to 1:3, and the agitator blades are straight.

[0016] Furthermore, in order to better achieve the heat exchange effect on the product at the top of the reactor, the cooling unit includes a C condenser and a C aftercooler. The upper ends of the first reactor and the second reactor are connected to the C condenser and the C aftercooler in sequence. The C condenser and / or the C aftercooler transport the third product to the finished product tank area as marine fuel oil through pipelines.

[0017] The present invention also provides a modular ethylene tar processing method, employing the aforementioned modular ethylene tar processing apparatus, comprising the following steps:

[0018] S1: Ethylene tar is preheated in the first preheater and then enters the first distillation column for vacuum distillation. The preheating temperature is 200℃-295℃, the vacuum degree of vacuum distillation is 10kPa-25kPa, and the temperature of vacuum distillation is 280℃-330℃. After some low-boiling-point components are vaporized, they are collected in the first reflux tank after heat exchange in the first heat exchange unit as the top product of the first column. Some unvaporized heavy components enter the bottom of the first distillation column as the bottom product of the first column.

[0019] S2: A portion of the product from the top of the first distillation column is refluxed back into the first distillation column. The other portion of the product from the top of the first distillation column is transported through pipelines to the finished product tank area as feedstock for catalytic hydrogenation diesel. The product from the bottom of the first distillation column is pumped to the first reboiler and the first evaporator, and then enters the upper part of the stripping section tray of the first distillation column for further heating, evaporation and separation. After staying for 1-20 hours, samples are taken for testing. Once the product from the bottom of the column is qualified, the first asphalt with a softening point of 100℃-150℃ is obtained.

[0020] S3: The first asphalt produced is preheated by the second preheater and then enters the second distillation column for vacuum distillation. The preheating temperature is 250℃-310℃. After some low-boiling-point components are vaporized, they are collected in the second reflux tank after heat exchange in the second heat exchange unit as the top product of the second column. Some unvaporized heavy components enter the bottom of the second distillation column and produce the second asphalt with a softening point of 120℃-180℃. The throughput of the first and second distillation columns is controlled by the flow control loop, and the throughput of the second distillation column is less than that of the first distillation column.

[0021] S4: A portion of the product from the top of the second distillation column is refluxed back into the second distillation column, and the other portion of the product from the top of the second distillation column is transported to the light oil receiving tank through a pipeline. The light oil receiving tank transports the second product to the finished product tank area through a pipeline as marine fuel oil. The produced second asphalt is pumped to the first reactor for reaction for 1-10 hours under the following conditions: vacuum degree 5kPa-20kPa, temperature 300℃-375℃ and continuous stirring. This yields the third asphalt with a softening point of 150℃-200℃ and the first light component. After the first light component is cooled by the cooling unit, the third product is transported to the finished product tank area through a pipeline as marine fuel oil.

[0022] S5: The produced third asphalt is pumped to the second reactor for reaction for 1-10 hours. The reaction conditions are vacuum degree 5kPa-20kPa, temperature 300℃-375℃ and continuous stirring to obtain the fourth asphalt and the second light component with a softening point of 180℃-220℃. After the second light component is cooled by the cooling unit, the third product is transported to the finished product tank area through pipeline as marine fuel oil.

[0023] S6: The produced fourth asphalt is pumped to a short-path molecular distillation unit for further separation and processing. The separation and processing conditions are a vacuum of 5 kPa-15 kPa and a temperature of 300℃-380℃, resulting in the fifth asphalt and the third light component with a softening point of 240℃-290℃. The third light component is cooled in a light component receiving tank and then the fourth product is transported to the finished product tank area through a pipeline as a rubber plasticizer.

[0024] S7: The produced fifth bitumen is cooled in a heavy component receiving tank, granulated by a granulation equipment, and then transported, packaged, and stored in a finished product warehouse.

[0025] S8: A portion of the first top product is transported to a precision distillation column via the first reflux tank. The precision distillation column further separates and cuts the product under vacuum conditions of 10kPa-30kPa and temperature of 200℃-330℃. Some low-boiling-point components vaporize and are collected in the third reflux tank after heat exchange in the third heat exchange unit, serving as the third top product. A portion of the third top product is refluxed back into the precision distillation column from the top. Another portion of the third top product is transported via pipeline to the finished product tank area as C9 product. Some unvaporized heavy components enter the bottom of the precision distillation column as the third bottom product. A portion of the third bottom product is transported to a reboiler and then refluxed back into the precision distillation column. Another portion of the third top product is transported via pipeline to the finished product tank area as feedstock for hydrotreated diesel after heat exchange in the fourth heat exchange unit.

[0026] Compared with the prior art, the beneficial technical effects of the present invention are as follows:

[0027] The modular ethylene tar processing apparatus and method of the present invention adopts a modular structural unit design, and can meet the user's requirements for different coated asphalts through different process combinations. The process adjustment is simple and the process flow can be adjusted as needed. At the same time, by setting up multiple reaction units, it can produce a variety of products such as hydrotreated diesel feedstock, marine fuel oil, rubber plasticizer, and 100℃-290℃ negative electrode coated asphalt, which can realize the comprehensive utilization of ethylene tar. The variety of products produced can greatly improve the comprehensive utilization value of ethylene tar. Furthermore, it can continuously separate light components, remove light components from the products, improve the product component distribution, and improve the asphalt coking value while maintaining the same softening point. Attached Figure Description

[0028] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0029] Figure 1 This is a schematic diagram of the modular ethylene tar processing apparatus of the present invention.

[0030] Explanation of reference numerals in the attached drawings: 1. First preheater; 2. First distillation column; 3. First reflux tank; 4. Second preheater; 5. Second distillation column; 6. Second reflux tank; 7. Light oil receiving tank; 8. First reactor; 9. Second reactor; 10. Short-path molecular distillation apparatus; 11. Heavy component receiving tank; 12. Light component receiving tank; 13. Granulator; 14. Bucket elevator; 15. Silo; 16. Packaging machine; 17. Precision distillation column; 18. Third reflux tank; 19. Reboiler; 20. Fourth heat exchanger; 21. B condenser; 22. B aftercooler; 23. First pump; 24. First reboiler; 25. First... 26. Evaporator; 27. Second reboiler; 28. Second evaporator; 29. ​​Preheater A; 30. Condenser A; 31. Preheater B; 32. Cooler B; 33. Condenser C; 34. Aftercooler C; 35. First transfer pump; 36. First reflux pump; 37. Second reflux pump; 38. Second transfer pump; 39. Third transfer pump; 40. Fourth transfer pump; 41. Fifth transfer pump; 42. Third reflux pump; 43. Bottom pump; 44. Condenser D; 45. Distillation column vacuum pump; 46. Reactor vacuum pump; 47. Short-path molecular vacuum pump; 48. Vacuum pump assembly; 49. Cold trap. Detailed Implementation

[0031] Embodiments of the present invention are described in detail below. Examples of these embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and are only used to explain the present invention, and should not be construed as limiting the present invention.

[0032] In the description of this invention, it should be understood that the terms "length," "width," "inner," and "outer," etc., indicating orientation or positional relationships based on the orientation or positional relationships shown in the accompanying drawings, are only for the convenience of describing the invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this invention, "a plurality of" means two or more, unless otherwise explicitly specified.

[0033] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0034] The technical solutions provided by the various embodiments of the present invention will be described in detail below with reference to the accompanying drawings.

[0035] Example 1

[0036] like Figure 1 As shown, the modular ethylene tar processing device of this embodiment 1 includes a first preheater 1, a first distillation column 2, a first heat exchange unit, a first reflux tank 3, a second preheater 4, a second distillation column 5, a second heat exchange unit, a second reflux tank 6, a light oil receiving tank 7, a first reaction vessel 8, a second reaction vessel 9, a cooling unit, a short-path molecular distillation apparatus 10, a heavy component receiving tank 11, a light component receiving tank 12, and granulation equipment. The first preheater 1 is connected to the first distillation column 2, the top of the first distillation column 2 is connected to the first heat exchange unit, the first heat exchange unit is connected to the first reflux tank 3, and the first reflux tank 3 is connected to the top of the first distillation column 2 through a first reflux pump 36. The first reflux tank 3 transports the first product to the finished product tank area as feedstock for catalytic hydrogenation diesel via the first reflux pump 36 and pipelines. Preferably, the first reflux tank 3 is a reflux tank with water-cutting and oil-separating functions, which can remove some of the water from the top product of the column.

[0037] Furthermore, the bottom of the first distillation column 2 is connected to the second preheater 4 via the first transfer pump 35, the second preheater 4 is connected to the second distillation column 5, the top of the second distillation column 5 is connected to the second heat exchange unit, the second heat exchange unit is connected to the second reflux tank 6, the second reflux tank 6 is connected to the top of the second distillation column 5 via the second reflux pump 37, the second reflux tank 6 is connected to the light oil receiving tank 7, the light oil receiving tank 7 is connected to the D condenser 44, the D condenser 44 is used to cool the output of the light oil receiving tank 7 and then transport the second output to the finished product tank area through pipeline as marine fuel oil.

[0038] Meanwhile, the bottom of the second distillation column 5 is connected to the first reactor 8 via the fourth transfer pump 40, the first reactor 8 is connected to the second reactor 9, and the upper ends of the first reactor 8 and the second reactor 9 are connected to a cooling unit. The cooling unit transports the third product to the finished product tank area as marine fuel oil through pipelines. The lower ends of the first reactor 8 and the second reactor 9 are connected to the granulation equipment via the second transfer pump 38 and the third transfer pump 39, respectively. It should be noted that the bottom of the first distillation column 2 is connected to the granulation equipment via the first transfer pump 35, and the bottom of the second distillation column 5 is connected to the granulation equipment via the fourth transfer pump 40, which can achieve... The bottom product of the first distillation column 2 or the second distillation column 5 is directly granulated by the granulation equipment. It should be noted that the granulation equipment includes a granulator 13, a bucket elevator 14, a silo 15, and a packaging machine 16. The corresponding product is transported to the granulator 13 by the corresponding conveying pump. The product of the granulator 13 is lifted into the silo 15 by the bucket elevator 14. The packaging machine 16 is located below the silo 15 to package the material in the silo 15. Preferably, the first reaction vessel 8 and the second reaction vessel 9 are slender with a length-to-diameter ratio between 1:2 and 1:3, and their agitator blades have a straight structure, which can reduce the backmixing of asphalt in the reaction vessel.

[0039] In this embodiment 1, the lower end of the second reaction vessel 9 is connected to the short-path molecular distillation unit 10 via the third transfer pump 39. The short-path molecular distillation unit 10 is connected to both the heavy component receiving tank 11 and the light component receiving tank 12. The heavy component receiving tank 11 is connected to the granulation equipment via the fifth transfer pump 41. It should be noted that the granulation equipment includes a granulator 13, a bucket elevator 14, a silo 15, and a packaging machine 16. The output of the heavy component receiving tank 11 is transported to the granulator 13 via the transfer pump. The output of the granulator 13 is lifted into the silo 15 via the bucket elevator 14. The packaging machine 16 is located below the silo 15 to package the materials within the silo 15. The light component receiving tank 12 transports the fourth output to the finished product tank area via pipeline as a rubber plasticizer.

[0040] In this embodiment 1, by adopting a modular structural unit design, different combinations of processes can meet the user's requirements for different coated asphalts. The process adjustment is simple, and the process flow can be adjusted as needed. At the same time, by setting up multiple reaction units, a variety of products can be produced, including hydrotreated diesel feedstock, marine fuel oil, rubber plasticizer, and 100℃-290℃ negative electrode coated asphalt. This enables the comprehensive utilization of ethylene tar, and the variety of products produced can greatly improve the comprehensive utilization value of ethylene tar. Furthermore, light components can be continuously separated and removed from the products, improving the product component distribution. Under the condition that the softening point of the produced products is the same, the asphalt coking value is also improved.

[0041] To more fully utilize ethylene tar, the system also includes a precision distillation column 17, a third heat exchange unit, and a third reflux tank 18. The first reflux tank 3 is connected to the precision distillation column 17 via a pipeline. The top of the precision distillation column 17 is connected to the third heat exchange unit, which is connected to the third reflux tank 18. The third reflux tank 18 is connected to the top of the precision distillation column 17 via a third reflux pump 42. The third reflux tank 18 transports the fifth product to the finished product tank area as C9 product via the third reflux pump 42 and pipeline. The bottom of the precision distillation column 17 is connected to a fourth heat exchange unit via a bottom pump 43. The fourth heat exchange unit is a fourth heat exchanger 20. The fourth heat exchanger 20 transports the sixth product to the finished product tank area as feedstock for hydrotreated diesel via pipeline. The bottom of the precision distillation column 17 is connected to a reboiler 19. The reboiler 19 refluxes the bottom product of the precision distillation column 17 back into the precision distillation column 17 via pipeline.

[0042] Furthermore, in order to better achieve the heat exchange effect on the top product of the precision distillation column 17, the third heat exchange unit includes a B condenser 21 and a B aftercooler 22. The top of the precision distillation column 17 is connected to the B condenser 21 and the B aftercooler 22 in sequence, and the B aftercooler 22 is connected to the third reflux tank 18.

[0043] In addition, a first pump 23 is connected to the bottom of the first distillation column 2. The first pump 23 is connected to a first reboiler 24 and a first evaporator 25 through pipes. The first reboiler 24 and the first evaporator 25 are connected to the upper part of the stripping section tray in the first distillation column 2 through pipes. A second pump 26 is connected to the bottom of the second distillation column 5. The second pump 26 is connected to a second reboiler 27 and a second evaporator 28 through pipes. The second reboiler 27 and the second evaporator 28 are connected to the upper part of the stripping section tray in the second distillation column 5 through pipes.

[0044] At this point, due to the configuration of the first reboiler 24 and the first evaporator 25, the unvaporized heavy components enter the bottom of the first distillation column 2, are pumped by the first pump 23 to the first reboiler 24 and the first evaporator 25, and then enter the upper part of the stripping section tray of the first distillation column 2. The kinetic energy of the rising gas phase propels the heavy components forward, and the gas and liquid phases flow in the same direction on the tray, reducing the liquid level difference. Simultaneously, it increases the gas flow velocity and the number of distribution points, increases the liquid surface area, and increases the probability of light components escaping. After the light components escape, the heavy components can accumulate in the bottom of the column, increasing the softening point of the asphalt in the bottom and narrowing the asphalt component distribution. This allows for a narrower distribution of asphalt components with the same softening point, resulting in more uniform coating during asphalt use and reducing the difficulty of treating tail gas caused by asphalt volatiles. The second reboiler 27 and the second evaporator 28 are configured on the same principle.

[0045] In order to achieve better heat exchange effect on the top product of the first distillation column 2, the first heat exchange unit includes an A preheater 29 and an A condenser 30, which are connected in sequence between the top of the first distillation column 2 and the first reflux tank 3.

[0046] In order to better achieve the heat exchange effect on the top product of the second distillation column 5, the second heat exchange unit includes a B preheater 31 and a B cooler 32, which are connected in sequence between the top of the second distillation column 5 and the second reflux tank 6.

[0047] In order to enable the working mode to be switched to the single distillation vessel working mode, the first distillation column 2 is connected to the first reaction vessel 8 and the second reaction vessel 9 through pipelines.

[0048] In this embodiment 1, by adopting a modular structural unit design, that is, the first distillation column 2, the second distillation column 5, the first reactor 8, and the second reactor 9 are connected by cross lines, different process combinations can be realized, such as one column and one reactor, two columns and one reactor, two columns and two reactors, and one column and two reactors. By combining different processes, the user's requirements for different coated asphalt can be met, and the process adjustment is simple.

[0049] Preferably, in order to better achieve the heat exchange effect on the product at the top of the reactor, the cooling unit includes a C condenser 33 and a C aftercooler 34. The upper ends of the first reactor 8 and the second reactor 9 are connected to the C condenser 33 and the C aftercooler 34 in sequence. The C condenser 33 and / or the C aftercooler 34 transport the third product to the finished product tank area as marine fuel oil through pipelines.

[0050] Furthermore, to further increase the coking value of the asphalt, the reboiler height of the first distillation column 2 and / or the second distillation column 5 is 5m-10m. Traditional distillation column reboiler height is approximately 2m. This technical solution designs the reboiler height of the first distillation column 2 and / or the second distillation column 5 to be 5m-10m, increasing the reboiler volume and improving the residence time of the asphalt in the column, thereby increasing the coking value of the asphalt.

[0051] Preferably, the jacket heating medium for the first distillation column 2, the second distillation column 5, the first reaction vessel 8, the second reaction vessel 9, and the short-path molecular distillation apparatus 10 can be heat transfer oil or molten salt. Heat transfer oil is more expensive but simple to operate, while molten salt is cheaper but has higher design requirements and is relatively more complex to operate.

[0052] The modular ethylene tar processing apparatus of this embodiment 1 also includes a distillation column vacuum pump 45 for evacuating the distillation column, a reaction vessel vacuum pump 46 for evacuating the reaction vessel, a short-range molecular vacuum pump 47 for evacuating the short-range molecular still, and a vacuum pump group 48 for evacuating the precision distillation column. A cold trap 49 is provided between the short-range molecular still 10 and the short-range molecular vacuum pump 47.

[0053] Example 2

[0054] The modular ethylene tar processing method of this embodiment 2, using the aforementioned modular ethylene tar processing apparatus, includes the following steps:

[0055] S1: Ethylene tar is preheated by the first preheater 1 and then enters the first distillation column 2 for vacuum distillation. Preferably, the preheating temperature is 200℃-295℃. More preferably, vacuum distillation is carried out under the conditions of vacuum degree of 10kPa-25kPa and temperature of 280℃-330℃. After some low-boiling-point components are vaporized, they are collected in the first reflux tank 3 after heat exchange in the first heat exchange unit as the first column top product. Some unvaporized heavy components enter the bottom of the first distillation column 2 as the first column bottom product.

[0056] S2: A portion of the product from the top of the first distillation column 2 is refluxed back into the first distillation column 2. The gas-liquid reflux forms a countercurrent gas-liquid two-phase flow on the packing surface, resulting in a relatively pure light component product at the top of the column. The other portion of the product from the top of the first column is transported through pipelines to the finished product tank area as feedstock for catalytic hydrogenation diesel. The product from the bottom of the first column is transported by the first pump 23 to the first reboiler 24 and the first evaporator 25, and then enters the upper part of the stripping section of the first distillation column 2 for further heating, evaporation and separation. After remaining for 1-20 hours, it is sampled and tested by the sampling port of the sampler. After the product from the bottom of the column is qualified, the first asphalt with a softening point of 100℃-150℃ is obtained.

[0057] The process utilizes the kinetic energy of rising gas to propel the heavy components forward and causes the gas and liquid phases to flow in the same direction on the trays, reducing the liquid level difference. This simultaneously increases the gas flow velocity and the number of distribution points, increases the liquid surface area, and increases the probability of light components escaping. After the light components escape, the heavy components can accumulate in the bottom of the tower, increasing the softening point of the asphalt in the bottom of the tower and narrowing the asphalt component distribution. This allows for a narrower distribution of asphalt components with the same softening point, resulting in more uniform coating during asphalt use and reducing the difficulty of treating exhaust gas caused by asphalt volatiles.

[0058] S3: The first asphalt produced is preheated by the second preheater 4 and then enters the second distillation column 5 for vacuum distillation. Preferably, the preheating temperature is 250℃-310℃. After some low-boiling-point components are vaporized, they are collected in the second reflux tank 6 after heat exchange in the second heat exchange unit as the top product of the second column. Some unvaporized heavy components enter the bottom of the second distillation column 5 and produce the second asphalt with a softening point of 120℃-180℃.

[0059] It should be noted that the principle of the second distillation column 5 is similar to that of the first distillation column 2. The throughput of the first distillation column 2 and the second distillation column 5 can be controlled by controlling the flow loop. Generally, the throughput of the second distillation column 5 is less than that of the first distillation column 2.

[0060] S4: A portion of the product from the top of the second distillation column 5 is refluxed back into the second distillation column 5. The other portion of the product from the top of the second distillation column is transported through a pipeline to the light oil receiving tank 7. The light oil receiving tank 7 transports the second product to the finished product tank area as marine fuel oil through a pipeline. The produced second asphalt is pumped to the first reactor 8 for reaction for 1-10 hours. Preferably, the reaction is carried out under the conditions of vacuum degree 5kPa-20kPa and temperature 300℃-375℃ with stirring to obtain the third asphalt and the first light component with a softening point of 150℃-200℃. After the first light component is cooled by the cooling unit, the third product is transported through a pipeline to the finished product tank area as marine fuel oil.

[0061] S5: The produced third asphalt is pumped to the second reactor 9 and reacted for 1-10 hours. Preferably, the reaction is carried out under vacuum of 5kPa-20kPa and temperature of 300℃-375℃ to obtain the fourth asphalt and the second light component with a softening point of 180℃-220℃. After the second light component is cooled by the cooling unit, the third product is transported to the finished product tank area through pipeline as marine fuel oil.

[0062] S6: The produced fourth asphalt is pumped to a short-path molecular distillation unit 10 for further separation. Preferably, the separation is carried out under vacuum conditions of 5 kPa-15 kPa and temperature of 300℃-380℃ to obtain a fifth asphalt with a softening point of 240℃-290℃ and a third light component. The third light component is cooled by a light component receiving tank 12, and then the fourth product is transported to the finished product tank area through a pipeline as a rubber plasticizer.

[0063] S7: The produced fifth bitumen is cooled by the heavy component receiving tank 11, granulated by the granulation equipment, and then transported, packaged and stored in the finished product warehouse.

[0064] S8: A portion of the first top product is transported to the precision distillation column 17 via the first reflux tank 3. After further cutting and separation in the precision distillation column 17, preferably under conditions of vacuum of 10kPa-30kPa and temperature of 200℃-330℃, some low-boiling-point components are vaporized and collected in the third reflux tank 18 after heat exchange in the third heat exchange unit as the third top product. A portion of the third top product is refluxed from the top of the precision distillation column 17 back into the precision distillation column 17. Another portion of the third top product is transported to the finished product tank area via pipeline as the fifth product as C9 product. Some unvaporized heavy components enter the bottom of the precision distillation column 17 as the third bottom product. A portion of the third bottom product is transported to the reboiler 19 and then refluxed back into the precision distillation column 17. Another portion of the third top product is transported to the finished product tank area via pipeline after heat exchange in the fourth heat exchange unit as the sixth product as the feedstock for hydrotreated diesel.

[0065] The embodiments described above are merely preferred embodiments of the present invention and are not intended to limit the scope of the present invention. Various modifications and improvements made by those skilled in the art to the technical solutions of the present invention without departing from the spirit of the present invention should fall within the protection scope defined by the claims of the present invention.

Claims

1. A modular ethylene tar processing apparatus, characterized in that, The system includes a first preheater, a first distillation column, a first heat exchange unit, a first reflux tank, a second preheater, a second distillation column, a second heat exchange unit, a second reflux tank, a light oil receiving tank, a first reactor, a second reactor, a cooling unit, a short-path molecular distillation apparatus, a heavy component receiving tank, a light component receiving tank, granulation equipment, a distillation column vacuum pump, a reactor vacuum pump, and a short-path molecular vacuum pump. The first preheater is connected to the first distillation column. The top of the first distillation column is connected to the first heat exchange unit, and the bottom is connected to the second preheater. The first heat exchange unit is connected to the first reflux tank, and the first reflux tank is connected to the top of the first distillation column. The first reflux tank transports the first product to the finished product tank area via pipeline as feedstock for catalytic hydrodiesel. The second preheater is connected to the second distillation column. The top of the second distillation column is connected to the second heat exchange unit, and the bottom is connected to the first reactor. The second heat exchange unit is connected to the second reflux tank, and the second reflux tank is connected to both the top of the second distillation column and the light oil receiving tank. The light oil receiving tank is connected via... The pipeline transports the second product to the finished product tank area as marine fuel oil. The distillation column vacuum pump is used to evacuate the first and second distillation columns. The first and second reaction vessels are connected, and the upper ends of both the first and second reaction vessels are connected to the cooling unit, while their lower ends are connected to the granulation equipment. The cooling unit transports the third product to the finished product tank area as marine fuel oil via pipeline. The reaction vessel vacuum pump is used to evacuate the first and second reaction vessels. The first distillation column is connected to the first and second reaction vessels via pipeline. The lower end of the second reaction vessel is connected to the short-path molecular still. The short-path molecular still is connected to the heavy component receiving tank and the light component receiving tank. The heavy component receiving tank is connected to the granulation equipment. The light component receiving tank transports the fourth product to the finished product tank area as a rubber plasticizer via pipeline. The short-path molecular vacuum pump is used to evacuate the short-path molecular still. A cold trap is provided between the short-path molecular still and the short-path molecular vacuum pump.

2. The modular ethylene tar processing apparatus according to claim 1, characterized in that, It also includes a precision distillation column, a third heat exchange unit, a third reflux tank, a fourth heat exchange unit, a reboiler, and a vacuum pump set. The first reflux tank is connected to the precision distillation column via a pipeline. The top of the precision distillation column is connected to the third heat exchange unit, and the bottom of the column is connected to the fourth heat exchange unit and the reboiler. The third reflux tank is connected to both the third heat exchange unit and the top of the precision distillation column. The third reflux tank transports the fifth product to the finished product tank area as C9 product via a pipeline. The fourth heat exchange unit transports the sixth product to the finished product tank area as feedstock for hydrotreated diesel via a pipeline. The reboiler refluxes the bottom product of the precision distillation column back into the precision distillation column via a pipeline. The vacuum pump set is used to evacuate the precision distillation column.

3. The modular ethylene tar processing apparatus according to claim 2, characterized in that, The third heat exchange unit includes a B condenser and a B aftercooler. The top of the precision distillation column is connected to the B condenser and the B aftercooler in sequence. The B aftercooler is connected to the third reflux tank.

4. The modular ethylene tar processing apparatus according to claim 1, characterized in that, The bottom of the first distillation column is connected to a first pump, which is connected to a first reboiler and a first evaporator via pipes. The first reboiler and the first evaporator are connected to the upper part of the stripping section tray in the first distillation column via pipes. The bottom of the second distillation column is connected to a second pump, which is connected to a second reboiler and a second evaporator via pipes. The second reboiler and the second evaporator are connected to the upper part of the stripping section tray in the second distillation column via pipes.

5. The modular ethylene tar processing apparatus according to claim 1, characterized in that, The first heat exchange unit includes an A preheater and an A condenser, which are connected sequentially between the top of the first distillation column and the first reflux tank.

6. The modular ethylene tar processing apparatus according to claim 1, characterized in that, The second heat exchange unit includes a B preheater and a B cooler, which are connected sequentially between the top of the second distillation column and the second reflux tank.

7. The modular ethylene tar processing apparatus according to claim 1, characterized in that, Both the first and second reactors are slender with a length-to-diameter ratio of 1:2 to 1:3, and the agitator blades are straight.

8. The modular ethylene tar processing apparatus according to any one of claims 1-7, characterized in that, The cooling unit includes a C condenser and a C aftercooler. The upper ends of the first reactor and the second reactor are connected to the C condenser and the C aftercooler in sequence. The C condenser and / or the C aftercooler transport the third product to the finished product tank area as marine fuel oil through pipelines.

9. A modular ethylene tar processing method, characterized in that, The modular ethylene tar processing apparatus according to any one of claims 1-8 includes the following steps: S1: Ethylene tar is preheated in the first preheater and then enters the first distillation column for vacuum distillation. The preheating temperature is 200℃-295℃, the vacuum degree of vacuum distillation is 10kPa-25kPa, and the temperature of vacuum distillation is 280℃-330℃. After some low-boiling-point components are vaporized, they are collected in the first reflux tank after heat exchange in the first heat exchange unit as the top product of the first column. Some unvaporized heavy components enter the bottom of the first distillation column as the bottom product of the first column. S2: A portion of the product from the top of the first distillation column is refluxed back into the first distillation column. The other portion of the product from the top of the first distillation column is transported through pipelines to the finished product tank area as feedstock for catalytic hydrogenation diesel. The product from the bottom of the first distillation column is pumped to the first reboiler and the first evaporator, and then enters the upper part of the stripping section tray of the first distillation column for further heating, evaporation and separation. After staying for 1-20 hours, samples are taken for testing. Once the product from the bottom of the column is qualified, the first asphalt with a softening point of 100℃-150℃ is obtained. S3: The first asphalt produced is preheated by the second preheater and then enters the second distillation column for vacuum distillation. The preheating temperature is 250℃-310℃. After some low-boiling-point components are vaporized, they are collected in the second reflux tank after heat exchange in the second heat exchange unit as the top product of the second column. Some unvaporized heavy components enter the bottom of the second distillation column and produce the second asphalt with a softening point of 120℃-180℃. The throughput of the first and second distillation columns is controlled by the flow control loop, and the throughput of the second distillation column is less than that of the first distillation column. S4: A portion of the product from the top of the second distillation column is refluxed back into the second distillation column, and the other portion of the product from the top of the second distillation column is transported to the light oil receiving tank through a pipeline. The light oil receiving tank transports the second product to the finished product tank area through a pipeline as marine fuel oil. The produced second asphalt is pumped to the first reactor for reaction for 1-10 hours under the following conditions: vacuum degree 5kPa-20kPa, temperature 300℃-375℃ and continuous stirring. This yields the third asphalt with a softening point of 150℃-200℃ and the first light component. After the first light component is cooled by the cooling unit, the third product is transported to the finished product tank area through a pipeline as marine fuel oil. S5: The produced third asphalt is pumped to the second reactor for reaction for 1-10 hours. The reaction conditions are vacuum degree 5kPa-20kPa, temperature 300℃-375℃ and continuous stirring to obtain the fourth asphalt and the second light component with a softening point of 180℃-220℃. After the second light component is cooled by the cooling unit, the third product is transported to the finished product tank area through pipeline as marine fuel oil. S6: The produced fourth asphalt is pumped to a short-path molecular distillation unit for further separation and processing. The separation and processing conditions are a vacuum of 5 kPa-15 kPa and a temperature of 300℃-380℃, resulting in the fifth asphalt and the third light component with a softening point of 240℃-290℃. The third light component is cooled in a light component receiving tank and then the fourth product is transported to the finished product tank area through a pipeline as a rubber plasticizer. S7: The produced fifth bitumen is cooled in a heavy component receiving tank, granulated by a granulation equipment, and then transported, packaged, and stored in a finished product warehouse. S8: A portion of the first top product is transported to a precision distillation column via the first reflux tank. The precision distillation column further separates and cuts the product under vacuum conditions of 10kPa-30kPa and temperature of 200℃-330℃. Some low-boiling-point components vaporize and are collected in the third reflux tank after heat exchange in the third heat exchange unit, serving as the third top product. A portion of the third top product is refluxed back into the precision distillation column from the top. Another portion of the third top product is transported via pipeline to the finished product tank area as C9 product. Some unvaporized heavy components enter the bottom of the precision distillation column as the third bottom product. A portion of the third bottom product is transported to a reboiler and then refluxed back into the precision distillation column. Another portion of the third top product is transported via pipeline to the finished product tank area as feedstock for hydrotreated diesel after heat exchange in the fourth heat exchange unit.

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