High-beta resin modified asphalt production system and process

Abstract

The invention belongs to the technical field of modified asphalt production, and particularly relates to a high-beta resin modified asphalt production system and process. A cleaning structure composed of a cleaning belt and other components is adopted at the bottom of the precipitation tank and used for slowly conveying heavy-phase oil deposited on a deposition slope in the sedimentation process downwards, the conveying speed is adjusted according to site conditions, and sedimentation layering cannot be affected by the adjusting principle. Therefore, the heavy-phase oil finally deposited on the slope surface cannot obtain enough bonding time to be collected to the bottom discharge port to be discharged, and the parking frequency is reduced. By adopting the composite heating furnace, the joint heating operation of the bottom circulation loops of the 1 # modification reaction kettle and the 2 # modification reaction kettle is realized, the space is saved, and the process is shortened.

Description

Technical Field

[0001] The present invention belongs to the technical field of modified asphalt production, and specifically relates to a high-β resin modified asphalt production system and process. Background Art

[0002] Coal tar is the residue after coal tar is distilled and extracted. Its output accounts for 50% to 60% of the total coal tar. It is a high-quality raw material for the carbon material industry and can be used to manufacture new high-value-added carbon materials, binders for graphite electrodes, and waterproof building materials. At present, high-quality asphalt is used as a modifier for commercial lithium-ion battery graphite negative electrode materials, making asphalt occupy a pivotal position in the lithium-ion battery negative electrode material industry.

[0003] By coating natural graphite with asphalt once or multiple times in liquid phase, the specific surface area of ​​graphite can be effectively reduced, thereby greatly improving the first reversible capacity and coulombic efficiency of graphite negative electrode materials and improving the cycle performance of batteries. The content of β-resin in coal tar pitch is one of the important indicators for evaluating the quality of asphalt, which directly affects the quality of new carbon materials.

[0004] CN201710640155.5 discloses a method for preparing high-β resin modified asphalt, using medium-temperature asphalt as raw material, obtaining refined asphalt with low quinoline insoluble content through solvent extraction and sedimentation separation, and then subjecting the refined asphalt to thermal polymerization-air oxidation modification treatment to obtain modified asphalt with high β resin content. This technology still has some problems, such as:

[0005] 1. During sedimentation separation, due to the certain viscosity of the heavy phase oil in the lower layer, a part of the heavy phase oil is still adhered to the bottom and cannot be cleaned after sedimentation separation. Over time, it is easy to block the heavy phase oil discharge port at the bottom, which may lead to shutdown operations. Once the shutdown occurs, the asphalt in the kettle will solidify and be difficult to clean, which will affect the production of modified asphalt.

[0006] 2. Most of the existing processes use multi-kettle and multi-furnace processes to produce modified asphalt, but the process is long, requires more equipment, is complex to operate, requires high investment, and occupies a large area. Summary of the invention

[0007] In order to solve the above technical problems, the inventors have obtained the technical solution of the present invention through practice and summary. The present invention adopts the following technical solution:

[0008] High β resin modified asphalt production system, including:

[0009] Raw material tank, which is connected to the pipeline of No. 1 reactor and transports medium-temperature asphalt to the mixing reactor;

[0010] A mixing reactor, wherein the mixing reactor is externally connected to a solvent tank via a pipeline;

[0011] A sedimentation tank, the feed inlet of which is connected to the discharge outlet of the mixing reactor, and a cleaning component is provided at the bottom of the sedimentation tank for cleaning the heavy phase oil in the lower layer;

[0012] The feed inlet of the distillation tower is connected to the upper clear phase oil outlet of the sedimentation tank, and the solvent vapor is drawn out from the top and refluxed into the solvent tank through the condenser;

[0013] A waste oil tank, wherein the feed port of the waste oil tank is connected to the lower heavy phase oil outlet of the sedimentation tank;

[0014] 1# reforming reactor, the feed inlet of the 1# reforming reactor is connected to the discharge outlet of the distillation tower, and the 1# reforming reactor is provided with a bottom circulation loop;

[0015] 2# reforming reactor, the feed inlet of 2# reforming reactor is connected with the discharge outlet of 1# reforming reactor, and 2# reforming reactor is provided with a bottom circulation loop;

[0016] A flash oil tank, the feed inlet of which is connected to the steam outlets of the 1# reforming reactor and the 2# reforming reactor;

[0017] The composite heating furnace heats the bottom circulation loop of the 1# reforming reactor, the 2# reforming reactor and the distillation tower to the required temperature;

[0018] The distillation heating furnace heats the bottom circulation loop of the distillation tower to a desired temperature;

[0019] Asphalt molding equipment, the feed inlet of the asphalt molding equipment is connected to the discharge port of the 2# reforming reactor.

[0020] With regard to the conventional mixing and stirring method of existing medium-temperature asphalt and dequinoline insoluble solvent oil, there is a problem that the medium-temperature asphalt is viscous and easy to stick to the wall in the initial stage, resulting in low mixing efficiency. It takes a long time to mix and stir to achieve sufficient mixing, resulting in a long process and low efficiency.

[0021] Preferably, the mixing reactor is provided with a left mixing chamber and a right centrifugal chamber, the left mixing chamber is used for atomizing and mixing the solvent oil and the medium-temperature asphalt to remove the quinoline insoluble matter, and the right centrifugal chamber is used for collecting and centrifugally treating the mixed mist;

[0022] The left mixing chamber is provided with an asphalt atomizing injection pipe, a dequinoline insoluble solvent injection pipe, a high-pressure airflow ring pipe, a collecting pipe, and an aeration pipe. The high-pressure airflow ring pipe is evenly provided with air nozzles for forming a high-pressure vortex airflow. The asphalt atomizing injection pipe and the dequinoline insoluble solvent injection pipe are symmetrically distributed and are both arranged toward the middle of the high-pressure vortex airflow.

[0023] The right centrifugal chamber is provided with a liquid collecting tank and a centrifugal device, the feed port of the liquid collecting tank is connected with the discharge port of the collecting pipe, the feed port of the centrifugal device is connected with the discharge port of the liquid collecting tank, and the discharge port is connected with the sedimentation tank.

[0024] Preferably, a plurality of collecting areas arranged obliquely downward in a stepped manner are provided on one side of the liquid collecting tank, a discharge port is provided on one side of the bottom, and a feed port is provided on the other side of the top.

[0025] Regarding question 1), preferably, inwardly recovering sedimentation slopes are provided on both sides of the bottom of the sedimentation tank, an anti-sedimentation port is provided on the sedimentation slope, and a directional conveying structure is installed on the outer side of the anti-sedimentation port, so that the lower layer heavy phase oil falling to the anti-sedimentation port is conveyed to the lower layer heavy phase oil discharge port through the directional conveying structure.

[0026] Preferably, the directional conveying structure includes a cleaning belt, a main conveying roller, an auxiliary conveying roller, and a motor group. The cleaning belt is made of anti-sticking and wear-resistant material. The main conveying roller and the auxiliary conveying roller are installed on the inner side of the cleaning belt, and the main conveying roller is connected to the output end of the motor group. The motor group is installed on the outer wall of the deposition slope.

[0027] Preferably, a scraper strip is installed at the bottom of the anti-deposition port to clean the belt surface;

[0028] Two mounting strips are arranged on the deposition slope, and the two mounting strips are respectively located on both sides of the cleaning belt. An adjusting rod is installed on the mounting strip, and a roller frame is mounted on the adjusting rod. The adjusting rod is used to adjust the distance between the roller frame and the deposition slope. A plurality of roller shafts are arranged on the roller frame at equal intervals along the cleaning direction of the cleaning belt. The roller shafts are rotatably installed on the roller frame, and the roller shafts act between the main conveying roller and the auxiliary conveying roller and are sealed to the cleaning belt at the anti-deposition port.

[0029] Preferably, a cleaning rack and a recovery tank are provided on the outer wall of the deposition slope, a flushing nozzle, a cleaning brush and a drying piece are installed on the cleaning rack, and the recovery tank is located below the bottom of the cleaning belt.

[0030] Regarding question 2), preferably, the composite heating furnace comprises a furnace body, in which circulation pipeline 1 and circulation pipeline 2 are arranged, circulation pipeline 1 is connected to the bottom circulation loop of No. 1 reforming reactor, and circulation pipeline 2 is connected to the bottom circulation loop of No. 2 reforming reactor.

[0031] In view of the problem that the existing asphalt reforming system is prone to generate asphalt slag and coking products in the kettle tube, preferably, the system also includes an anthracene oil-wash oil introduction pipe, which is installed in the bottom circulation loop of the 1# reforming reactor and the 2# reforming reactor through a control valve. By lowering the temperature after the anthracene oil-wash oil is added, the ideal viscosity can be achieved, and the generation of coking products and asphalt slag can be prevented. The temperature of the reforming kettle is also appropriately lowered. Since the temperature reduction is bound to affect the reforming effect, the anthracene oil-wash oil can enhance the generation of TI, reduce the viscosity of the material, and reduce the asphalt slag and coking products caused by the ash content, thereby further improving the β value.

[0032] The production process of high-β resin modified asphalt includes:

[0033] Step 1, raw material-solvent mixing

[0034] The medium-temperature asphalt is delivered from the raw material tank to the left mixing chamber of the mixing reactor through a pipeline. The high-pressure airflow ring pipe is connected to a nitrogen source and forms a high-pressure vortex airflow through a gas nozzle. The medium-temperature asphalt is sprayed obliquely upward with the middle of the high-pressure vortex airflow through the asphalt atomization injection pipe and the dequinoline insoluble solvent through the dequinoline insoluble solvent injection pipe. The confluence direction is the direction of the collecting pipe toward the center. The middle area of ​​the high-pressure vortex airflow is in a negative pressure state and is introduced into the collecting pipe in accordance with the confluence direction;

[0035] Step 2, collection and centrifugation

[0036] The atomized mixed steam after confluence is collected in the collecting area of ​​the liquid collecting tank and then flows into the centrifugal device for centrifugal treatment and then transported to the sedimentation tank;

[0037] Step 3, Separation by Sedimentation

[0038] The solution in step 2 is precipitated and separated in a precipitation tank to form an upper clear phase oil and a lower heavy phase oil;

[0039] The upper light phase oil is sent to the distillation tower, and the solvent vapor of the quinoline-insoluble matter is drawn out from the top and refluxed into the solvent tank through the condenser;

[0040] Step 4: Asphalt Modification

[0041] The remaining bottom oil in the distillation tower is sent to the 1# reforming reactor for β reforming, and the remaining part is heated up in the distillation heating furnace through the bottom circulation loop and refluxed to the distillation tower. The remaining bottom oil in the 1# reforming reactor is sent to the 2# reforming reactor for α reforming, and the remaining part is heated up in the composite heating furnace through the bottom circulation loop and refluxed to the 1# reforming reactor. The remaining bottom oil in the 2# reforming reactor is sent to the asphalt molding equipment for molding treatment or into the high-position asphalt tank, and the remaining part is heated up in the composite heating furnace through the bottom circulation loop and refluxed to the 2# reforming reactor;

[0042] The flash oil vapor in the 1# reforming reactor and the 2# reforming reactor enters the flash oil tank for cooling.

[0043] Compared with the prior art, the present invention has the following beneficial effects:

[0044] 1. The present invention aims at problem 1. The bottom of the sedimentation tank adopts a cleaning structure composed of cleaning belts and other components to slowly transport the heavy phase oil deposited on the sedimentation slope during the sedimentation process downward. The conveying speed is adjusted according to the on-site conditions. The adjustment principle cannot affect the sedimentation stratification. The heavy phase oil on the sedimentation slope cannot get enough bonding time and is collected at the bottom discharge port for discharge, so as to reduce the parking frequency.

[0045] 2. In response to problem 2, the present invention adopts a composite heating furnace to achieve the common heating operation of the bottom circulation loops of the 1# reforming reactor and the 2# reforming reactor, thereby saving space and shortening the process.

[0046] 3. The present invention is directed to the conventional mixing and stirring method of the existing medium-temperature asphalt and the dequinoline insoluble solvent oil, which has the problem that the medium-temperature asphalt is viscous and easy to stick to the wall in the initial stage, resulting in low mixing efficiency, and requires a long time of mixing and stirring to complete sufficient mixing, resulting in a long process and low efficiency. A new type of counter-spraying confluence method is adopted, and a high-pressure airflow is used on the outside of the counter-spraying confluence to make a relative negative pressure environment appear inside, thereby realizing that the confluence enters the collection tank through the collection pipe and enters the centrifugal device for centrifugal treatment. BRIEF DESCRIPTION OF THE DRAWINGS

[0047] Figure 1 It is a schematic diagram of the production system structure of the present invention.

[0048] Figure 2 This is a structural distribution diagram of the mixed reaction tower of the present invention.

[0049] Figure 3 for Figure 2 Bottom view of the structure of medium and high pressure airflow ring pipe and collecting pipe.

[0050] Figure 4 It is the internal structure distribution diagram of the sedimentation tank of the present invention.

[0051] Figure 5 for Figure 4 A local structural diagram of the cleanup structure.

[0052] Figure 6 This is the structural distribution diagram on the side wall of the sedimentary slope.

[0053] Figure 7 This is the internal structure diagram of the composite heating furnace. DETAILED DESCRIPTION

[0054] The technical solutions in the embodiments of the present invention will be described clearly and completely below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, rather than all the embodiments.

[0055] In the description of the present invention, it is necessary to understand that the terms "upper", "lower", "front", "back", "left", "right", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship are based on the orientation or position relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention.

[0056] like Figure 1 As shown, the high β resin modified asphalt production system includes:

[0057] The raw material tank 10 is connected to the pipeline of the 1# reactor and transports the medium-temperature asphalt into the mixing reactor 20;

[0058] A mixing reactor 20, wherein the mixing reactor 20 is connected to a solvent tank 40 via a pipeline;

[0059] A sedimentation tank 50, the feed port of the sedimentation tank 50 is connected to the discharge port of the mixing reactor 20, and a cleaning component is provided at the bottom of the sedimentation tank 50 for cleaning the heavy phase oil in the lower layer;

[0060] The distillation tower 70, the feed inlet of the distillation tower 70 is connected to the upper clear phase oil outlet of the sedimentation tank 50, and the solvent vapor is drawn out from the top and refluxed into the solvent tank through the condenser;

[0061] A waste oil tank 60, wherein the feed port of the waste oil tank 60 is connected to the lower heavy phase oil outlet of the sedimentation tank 50;

[0062] 1# reforming reactor 80, the feed inlet of 1# reforming reactor 80 is connected to the discharge outlet of distillation tower 70, and 1# reforming reactor 80 is provided with a bottom circulation loop;

[0063] 2# reforming reactor 90, the feed inlet of 2# reforming reactor 90 is connected to the discharge outlet of 1# reforming reactor 80, and 2# reforming reactor 90 is provided with a bottom circulation loop;

[0064] A flash oil tank 110, wherein the feed port of the flash oil tank 110 is connected to the steam outlets of the first reforming reactor 80 and the second reforming reactor 90;

[0065] The composite heating furnace 100 heats the bottom circulation loop of the 1# reforming reactor 80, the 2# reforming reactor 90 and the distillation tower 70 to a desired temperature;

[0066] The distillation heating furnace 30 heats the bottom circulation loop of the distillation tower 70 to a desired temperature;

[0067] Asphalt molding equipment, the feed inlet of the asphalt molding equipment is connected to the discharge port of the 2# reforming reactor 90.

[0068] In this embodiment, the mixing reactor can be implemented by a conventional stirring and mixing method, and the sedimentation tank only has a cleaning component added to the bottom to achieve bottom cleaning.

[0069] During implementation, the medium-temperature asphalt is pumped from the raw material tank 10 into the mixing reactor 20, mixed with the dequinoline insoluble solvent oil in the solvent tank 40 in the mixing reactor 20 to obtain a mixed solution (containing insoluble matter), which is then sent to the precipitation tank 50, and after sedimentation and stratification, an upper clear phase oil and a lower heavy phase oil are formed. The upper light phase oil is sent to the distillation tower 70, and the dequinoline insoluble solvent vapor is drawn out from the top and refluxed into the solvent tank 40 through the condenser; the lower heavy phase oil enters the waste oil tank 60 through the discharge port.

[0070] A small portion of the remaining bottom oil in the distillation tower 70 is sent to the No. 1 modification reactor 80 for β modification, and the rest of the majority is heated up and refluxed to the distillation tower 70 through the bottom circulation loop in the distillation heating furnace 30; a small portion of the remaining bottom oil in the No. 1 modification reactor 80 is sent to the No. 2 modification reactor 90 for α modification, and the rest of the majority is heated up and refluxed to the No. 1 modification reactor 80 through the bottom circulation loop in the composite heating furnace 100; a small portion of the remaining bottom oil in the No. 2 modification reactor 90 is sent to the asphalt molding equipment for molding treatment, and the rest of the majority is heated up and refluxed to the No. 2 modification reactor 90 through the bottom circulation loop in the composite heating furnace 100.

[0071] The flash oil vapor in the 1# reforming reactor and the 2# reforming reactor enters the flash oil tank for cooling.

[0072] On the basis of the above embodiment, the conventional mixing and stirring method of the existing medium-temperature asphalt and the dequinoline insoluble solvent oil has the problem that the medium-temperature asphalt is viscous and easy to stick to the wall in the initial stage, resulting in low mixing efficiency. It takes a long time to mix and stir to complete sufficient mixing, resulting in a long process and low efficiency. The following improvements are made:

[0073] The mixing reactor 20 is provided with a left mixing chamber 21 and a right centrifugal chamber 22. The left mixing chamber 21 is used for atomizing and mixing the solvent oil and the medium-temperature asphalt to remove the quinoline insoluble matter, and the right centrifugal chamber 22 is used for collecting and centrifugally treating the mixed mist.

[0074] like Figure 2 and Figure 3As shown, in the left mixing chamber 21, a pitch atomizing jet pipe 211, a de-quinoline insoluble solvent jet pipe 213, a high-pressure airflow annular pipe 212, a collecting pipe 214, and an aeration pipe 215 are provided, the high-pressure airflow annular pipe 212 is connected to an external nitrogen source and is evenly distributed with a gas nozzle thereon, the gas nozzle is used to form a high-pressure vortex airflow, and the pitch atomizing jet pipe 211 and the de-quinoline insoluble solvent jet pipe 213 are symmetrically distributed and are all arranged towards the middle part of the high-pressure vortex airflow. The confluence of the spray is atomized, and the high-pressure vortex airflow of the outside is isolated to avoid overflowing, and a swirl eye is also formed inside the airflow simultaneously, and a certain degree of negative pressure phenomenon occurs inside, and is delivered to the right centrifugal chamber 22 through a collecting tank 214.

[0075] The right centrifugal chamber 22 is provided with a liquid collecting tank 221 and a centrifugal device 222. The feed port of the liquid collecting tank 221 is connected to the discharge port of the collecting pipe 214. One side of the liquid collecting tank 221 is provided with a plurality of stepped downwardly arranged collecting areas. The bottom side is provided with a discharge port, and the other side of the top is provided with a feed port. The feed port of the centrifugal device 222 is connected to the discharge port of the liquid collecting tank 221, and the discharge port is connected to the sedimentation tank 50. The bottom of the left mixing chamber 21 is provided with a collection area, which is connected to the liquid collecting tank 221 through a delivery pump and a pipeline.

[0076] The collected atomized liquid flows downward along the collection area to the centrifugal device 222 to complete centrifugation, and then is sent to the sedimentation tank 50.

[0077] In view of the problem that the heavy phase oil in the lower layer is easy to stick to the bottom of the sedimentation tank during sedimentation separation, which is prone to stoppage, the following improvements are made:

[0078] like Figure 4 , 5 As shown in Figure 6, both sides of the bottom of the sedimentation tank 50 are provided with inwardly recovering sedimentation slopes 51, and an anti-sedimentation port 52 is provided on the sedimentation slope 51. A directional conveying structure is installed on the outer side of the anti-sedimentation port 52, and the lower layer heavy phase oil falling to the anti-sedimentation port 52 is conveyed to the lower layer heavy phase oil discharge port through the directional conveying structure.

[0079] The directional conveying structure includes a cleaning belt 53, a main conveying roller 54, an auxiliary conveying roller 55, and a motor group 56. The cleaning belt 53 is made of anti-sticking and wear-resistant material (for example, wear-resistant polytetrafluoroethylene material). The main conveying roller 54 and the auxiliary conveying roller 55 are installed on the inner side of the cleaning belt 53, and the main conveying roller 54 is connected to the output end of the motor group 56. The motor group 56 is installed on the outer wall of the deposition slope 51.

[0080] An inward-retracted deposition slope 51 is set at the bottom to complete the deposition collection, and a cleaning belt 53 is used to transport the heavy phase oil settled thereon downward, thereby shortening the time of the heavy phase oil on the deposition slope, reducing the degree of adhesion, accelerating the deposition efficiency, slowing down the deposition time, extending the parking cycle, and avoiding blockage at the bottom.

[0081] In the above embodiment, in order to recover the heavy phase oil as much as possible, the following improvements are made: a scraper strip 57 is installed at the bottom of the anti-sedimentation port 52 to process the surface of the cleaning belt 53 .

[0082] In the above embodiment, in order to solve the problem that the cleaning belt is easy to be poorly sealed with the anti-deposition port, the following improvements are made: two mounting strips 58 are arranged on the deposition slope 51, and the two mounting strips 58 are respectively located on both sides of the cleaning belt 53, and an adjusting rod 59 is installed on the mounting strip 58, and a roller frame 510 is mounted on the adjusting rod 59. By adjusting the adjusting rod 59, the spacing between the roller frame 510 and the deposition slope 51 is adjusted. A plurality of roller shafts 511 are arranged on the roller frame 510 at equal intervals along the cleaning direction of the cleaning belt 53, and the roller shafts 511 are rotatably mounted on the roller frame 510. The roller shafts 511 act between the main conveying roller 54 and the auxiliary conveying roller 55 and seal the cleaning belt 53 at the anti-deposition port 52. The strength of the roller shaft 511 squeezing the cleaning belt 53 by adjusting the adjusting rod 59 ensures the sealing effect.

[0083] In the above embodiment, in order to solve the problem that the cleaning belt surface is prone to residual oil, the following improvements are made: a cleaning frame 512 and a recovery groove 513 are provided on the outer wall of the deposition slope 51, a flushing nozzle 514, a cleaning brush 515 and a drying member 516 are installed on the cleaning frame 512, and the recovery groove 513 is located below the bottom of the cleaning belt 53. The surface cleaning of the cleaning belt 53 is completed in sequence by flushing, cleaning (soft hair) and air drying.

[0084] In the above embodiment, in order to solve the problem of producing modified asphalt with traditional multi-kettle and multi-furnace process, which has a long process, many equipments, complicated operation, high investment and large land area, the following improvements are made: the composite heating furnace 100 includes a furnace body, and a circulation pipeline 101 and a circulation pipeline 2 102 are arranged in the furnace body. The circulation pipeline 101 is connected to the bottom circulation loop of the 1# modified reactor 80, and the circulation pipeline 2 102 is connected to the bottom circulation loop of the 2# modified reactor 90.

[0085] In view of the problem that the existing asphalt reforming system is prone to generate asphalt slag and coking products in the kettle tube, preferably, the system also includes an anthracene oil-wash oil introduction pipe, which is installed through a control valve in the bottom circulation loop of the 1# reforming reactor 80 and the 2# reforming reactor 90. By lowering the temperature after the anthracene oil-wash oil is added, the ideal viscosity can be achieved, the generation of coking products and asphalt slag can be prevented, and the temperature of the reforming kettle can be appropriately lowered. Since the temperature reduction is bound to affect the reforming effect, the anthracene oil-wash oil can enhance the generation of TI, reduce the viscosity of the material, reduce the asphalt slag and coking products caused by the ash content, and further increase the β value.

[0086] The production process of high-β resin modified asphalt includes:

[0087] Step 1, raw material-solvent mixing

[0088] The medium-temperature asphalt is delivered from the raw material tank 10 to the left mixing chamber 21 of the mixing reactor 20 through a pipeline. The high-pressure airflow ring pipe 212 is externally connected to a nitrogen source and forms a high-pressure vortex airflow through a gas nozzle. The medium-temperature asphalt is sprayed obliquely upward with the middle part of the high-pressure vortex airflow through the asphalt atomization injection pipe 211 and the dequinoline insoluble solvent through the dequinoline insoluble solvent injection pipe 213. The confluence direction is the direction of the collecting pipe 214 toward the center. The middle area of ​​the high-pressure vortex airflow is in a negative pressure state, and is introduced into the collecting pipe 214 in accordance with the confluence direction;

[0089] Step 2, collection and centrifugation

[0090] The merged atomized mixed steam is collected in the collecting area of ​​the liquid collecting tank 221 and then flows into the centrifugal device 222 for centrifugal treatment and then transported to the sedimentation tank 50.

[0091] Step 3, Separation by Sedimentation

[0092] The solution in step 2 is precipitated and separated in the precipitation tank 50 to form an upper clear phase oil and a lower heavy phase oil;

[0093] The upper light phase oil is sent to the distillation tower 70, and the solvent vapor of the quinoline-insoluble matter is drawn out from the top and refluxed into the solvent tank through the condenser;

[0094] Step 4: Asphalt Modification

[0095] The remaining bottom oil in the distillation tower 70 is sent to the 1# reforming reactor 80 for β reforming, and the remaining part is heated and refluxed to the distillation tower 70 through the bottom circulation loop in the distillation heating furnace 30. The remaining bottom oil in the 1# reforming reactor 80 is sent to the 2# reforming reactor 90 for α reforming, and the remaining part is heated and refluxed to the 1# reforming reactor 80 through the bottom circulation loop in the composite heating furnace 100. The remaining bottom oil in the 2# reforming reactor 90 is sent to the asphalt molding equipment for molding treatment or into the high-position asphalt tank, and the remaining part is heated and refluxed to the 2# reforming reactor 90 through the bottom circulation loop in the composite heating furnace 100;

[0096] The flashed oil vapor in the 1# reforming reactor 80 and the 2# reforming reactor 90 enters the flashed oil tank 110 for cooling.

[0097] The indexes of the modified asphalt prepared are softening point 106-112°C, toluene insoluble matter 28-39%, quinoline insoluble matter 6-14%, beta resin>20%, coking value>57%, and ash content<0.1%.

[0098] The above is only a preferred specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. The replacement may be a replacement of a part of the structure, device, method step, or a complete technical solution. Any equivalent replacement or change according to the technical solution and the inventive concept of the present invention shall be covered within the protection scope of the present invention.

Claims

1. High β resin modified asphalt production system, characterized in that: include: Raw material tank, which is connected to the pipeline of No. 1 reactor and transports medium-temperature asphalt to the mixing reactor; A mixing reactor, wherein the mixing reactor is externally connected to a solvent tank via a pipeline; A sedimentation tank, the feed inlet of which is connected to the discharge outlet of the mixing reactor, and a cleaning component is provided at the bottom of the sedimentation tank for cleaning the heavy phase oil in the lower layer; The feed inlet of the distillation tower is connected to the upper clear phase oil outlet of the sedimentation tank, and the solvent vapor is drawn out from the top and refluxed into the solvent tank through the condenser; A waste oil tank, wherein the feed port of the waste oil tank is connected to the lower heavy phase oil outlet of the sedimentation tank; 1# reforming reactor, the feed inlet of the 1# reforming reactor is connected to the discharge outlet of the distillation tower, and the 1# reforming reactor is provided with a bottom circulation loop; 2# reforming reactor, the feed inlet of 2# reforming reactor is connected with the discharge outlet of 1# reforming reactor, and 2# reforming reactor is provided with a bottom circulation loop; A flash oil tank, the feed inlet of which is connected to the steam outlets of the 1# reforming reactor and the 2# reforming reactor; The composite heating furnace heats the bottom circulation loop of the 1# reforming reactor, the 2# reforming reactor and the distillation tower to the required temperature; The distillation heating furnace heats the bottom circulation loop of the distillation tower to a desired temperature; Asphalt molding equipment, the feed inlet of the asphalt molding equipment is connected to the discharge port of the 2# reforming reactor.

2. The high-β resin modified asphalt production system according to claim 1, characterized in that: The mixing reactor is provided with a left mixing chamber and a right centrifugal chamber, the left mixing chamber is used for atomizing and mixing the solvent oil and the medium-temperature asphalt to remove the quinoline insoluble matter, and the right centrifugal chamber is used for collecting and centrifuging the mixed mist; The left mixing chamber is provided with an asphalt atomizing injection pipe, a dequinoline insoluble solvent injection pipe, a high-pressure airflow ring pipe, a collecting pipe, and an aeration pipe. The high-pressure airflow ring pipe is evenly provided with air nozzles for forming a high-pressure vortex airflow. The asphalt atomizing injection pipe and the dequinoline insoluble solvent injection pipe are symmetrically distributed and are both arranged toward the middle of the high-pressure vortex airflow. The right centrifugal chamber is provided with a liquid collecting tank and a centrifugal device, the feed port of the liquid collecting tank is connected with the discharge port of the collecting pipe, the feed port of the centrifugal device is connected with the discharge port of the liquid collecting tank, and the discharge port is connected with the sedimentation tank.

3. The high-β resin modified asphalt production system according to claim 2, characterized in that: One side of the liquid collecting tank is provided with a plurality of step-shaped collecting areas which are arranged obliquely downward, one side of the bottom is provided with a discharge port, and the other side of the top is provided with a feed port.

4. The high-β resin modified asphalt production system according to claim 3, characterized in that: The bottom of the sedimentation tank is provided with inwardly recovering sedimentation slopes on both sides, and an anti-sedimentation port is provided on the sedimentation slope. A directional conveying structure is installed outside the anti-sedimentation port, and the lower layer heavy phase oil falling to the anti-sedimentation port is conveyed to the lower layer heavy phase oil discharge port through the directional conveying structure.

5. The high-β resin modified asphalt production system according to claim 4, characterized in that: The directional conveying structure includes a cleaning belt, a main conveying roller, an auxiliary conveying roller, and a motor group. The cleaning belt is made of anti-sticking and wear-resistant material. The main conveying roller and the auxiliary conveying roller are installed on the inner side of the cleaning belt, and the main conveying roller is connected to the output end of the motor group. The motor group is installed on the outer wall of the deposition slope.

6. The high-β resin modified asphalt production system according to claim 5, characterized in that: A scraper is installed at the bottom of the anti-deposition port to clean the belt surface; Two mounting strips are arranged on the deposition slope, and the two mounting strips are respectively located on both sides of the cleaning belt. An adjusting rod is installed on the mounting strip, and a roller frame is mounted on the adjusting rod. The adjusting rod is used to adjust the distance between the roller frame and the deposition slope. A plurality of roller shafts are arranged on the roller frame at equal intervals along the cleaning direction of the cleaning belt. The roller shafts are rotatably installed on the roller frame, and the roller shafts act between the main conveying roller and the auxiliary conveying roller and are sealed to the cleaning belt at the anti-deposition port.

7. The high-β resin modified asphalt production system according to claim 6, characterized in that: A cleaning frame and a recovery tank are arranged on the outer wall of the deposition slope, a flushing nozzle, a cleaning brush and a drying piece are installed on the cleaning frame, and the recovery tank is located below the bottom of the cleaning belt.

8. The high-β resin modified asphalt production system according to claim 7, characterized in that: The composite heating furnace comprises a furnace body, in which a circulation pipeline 1 and a circulation pipeline 2 are arranged. The circulation pipeline 1 is connected to the bottom circulation loop of the 1# reforming reactor, and the circulation pipeline 2 is connected to the bottom circulation loop of the 2# reforming reactor.

9. The high-β resin modified asphalt production system according to claim 8, characterized in that: The system also includes an anthracene oil-wash oil introduction pipe, which is installed in the bottom circulation loop of the No. 1 reforming reactor and the No. 2 reforming reactor through a control valve.

10. A process for producing high-β resin modified asphalt, using the production system as claimed in claim 9, characterized in that: include: Step 1, raw material-solvent mixing The medium-temperature asphalt is delivered from the raw material tank to the left mixing chamber of the mixing reactor through a pipeline. The high-pressure airflow ring pipe is connected to a nitrogen source and forms a high-pressure vortex airflow through a gas nozzle. The medium-temperature asphalt is sprayed obliquely upward with the middle of the high-pressure vortex airflow through the asphalt atomization injection pipe and the dequinoline insoluble solvent through the dequinoline insoluble solvent injection pipe. The confluence direction is the direction of the collecting pipe toward the center. The middle area of ​​the high-pressure vortex airflow is in a negative pressure state and is introduced into the collecting pipe in accordance with the confluence direction; Step 2, collection and centrifugation The atomized mixed steam after confluence is collected in the collecting area of ​​the liquid collecting tank and then flows into the centrifugal device for centrifugal treatment and then transported to the sedimentation tank; Step 3, Separation by Sedimentation The solution in step 2 is precipitated and separated in a precipitation tank to form an upper clear phase oil and a lower heavy phase oil; The upper light phase oil is sent to the distillation tower, and the solvent vapor of the quinoline-insoluble matter is drawn out from the top and refluxed into the solvent tank through the condenser; Step 4: Asphalt Modification The remaining bottom oil in the distillation tower is sent to the 1# reforming reactor for β reforming, and the remaining part is heated up in the distillation heating furnace through the bottom circulation loop and refluxed to the distillation tower. The remaining bottom oil in the 1# reforming reactor is sent to the 2# reforming reactor for α reforming, and the remaining part is heated up in the composite heating furnace through the bottom circulation loop and refluxed to the 1# reforming reactor. The remaining bottom oil in the 2# reforming reactor is sent to the asphalt molding equipment for molding treatment, and the remaining part is heated up in the composite heating furnace through the bottom circulation loop and refluxed to the 2# reforming reactor; The flash oil vapor in the 1# reforming reactor and the 2# reforming reactor enters the flash oil tank for cooling.

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