Continuous high-softening-point spinnable asphalt production device

Abstract

The utility model discloses a continuous high-softening-point spinnable asphalt production device which comprises a rectifying tower I, a rectifying tower II and a rectifying tower III which are sequentially connected in series and are respectively connected with a rectifying tower vacuum pump, a reaction system I is respectively connected with the rectifying tower II and the rectifying tower III, and a reaction system II is connected with the reaction system I in series / in parallel. The second reaction system is connected with the second rectifying tower, the first reaction system and the second reaction system are both connected with the first slivering packaging system, and the second rectifying tower and the third rectifying tower are both connected with the second slivering packaging system. According to the utility model, the towers and the kettles are connected in series and in parallel, so that the processing amount can be improved on the premise of realizing low energy consumption, and high-softening-point spinnable asphalt can be simultaneously produced by a plurality of production lines. In view of the structures of the rectifying tower and the reaction kettle, the aim of higher coking value of asphalt at the same softening point can be achieved.

Description

Technical Field

[0001] The utility model relates to the technical field of high-softening-point spinnable asphalt, in particular to a continuous production device of high-softening-point spinnable asphalt. Background Art

[0002] In the prior art, a Chinese patent application with application number CN202211296166.3, entitled "An Ethylene Tar Comprehensive Processing Device and Method", was applied for by Chengdu Yutai New Materials Technology Co., Ltd., which disclosed that ethylene tar was subjected to two vacuum distillations and two reactors for thermal polycondensation and then passed through a short-range molecular distiller to obtain a high softening point spinnable asphalt. This utility model was also applied for by Chengdu Yutai New Materials Technology Co., Ltd., and it is an upgrade on the original technology to solve many problems of the original process, which can solve but not limited to the following problems.

[0003] The asphalt softening point index reflects the temperature sensitivity of asphalt. Temperature sensitivity refers to the property that the viscosity and plasticity of petroleum asphalt change with the rise and fall of temperature. Asphalt with low temperature sensitivity has less change in viscosity and plasticity with the rise and fall of temperature. Temperature sensitivity is expressed by softening point, which is the temperature at which asphalt changes from a solid state to a paste with a certain fluidity when heated. The higher the softening point, the lower the temperature sensitivity of asphalt. The original processing capacity is subject to the vacuum distillation system - the gas phase load at the top of the distillation tower. When the processing capacity is at full load, the product cannot reach the required softening point, and the product stability cannot be effectively guaranteed, resulting in limited processing capacity under the premise of ensuring product quality.

[0004] There is a problem that the two main indicators for determining whether high softening point spinnable asphalt is a qualified product are not corresponding. In the original technology, the heating medium of the reactor is high-temperature heat transfer oil, and the main component of the high-temperature heat transfer oil is hydrogenated terphenyl. Due to the physical and chemical properties of the heat transfer oil, the operating temperature of the reaction system is not more than 330°C, causing the coking value of the product to be lower than the indicator corresponding to the corresponding softening point.

[0005] The original technology has a short reaction residence time and the thermal polycondensation reaction is not complete. It is necessary to use a short-range molecular distiller to produce products with high softening point and high coking value. Utility Model Content

[0006] In order to solve the above problems, the utility model provides a continuous production device of high-softening-point spinnable asphalt.

[0007] In order to solve the above technical problems, the technical solution of the utility model is: a continuous high softening point spinnable asphalt production device, comprising a distillation tower 1, a distillation tower 2, and a distillation tower 3 connected in series in sequence, and respectively connected to the distillation tower vacuum pump, a reaction system 1 is connected to the distillation tower 2 and the distillation tower 3 respectively, the reaction system 2 is connected in series / parallel with the reaction system 1, the reaction system 2 is connected to the distillation tower 2, the reaction system 1 and the reaction system 2 are both connected to the strip making and packaging system 1, and the distillation tower 2 and the distillation tower 3 are both connected to the strip making and packaging system 2;

[0008] The distillation tower 1 includes a distillation tower body 1, the distillation tower body 1 is connected to a tower preheater, the tower preheater is connected to a distillation tower 2, the distillation tower body 1, a tower circulation pump, and a tower reboiler are connected in a circular manner in sequence, the distillation tower body 1, a tower delivery pump, a tower preheater, and a distillation tower 2 are connected in sequence, the distillation tower body 1, a tower condenser, a tower reflux tank, and a tower reflux pump are connected in a circular manner in sequence, and the tower reflux tank is connected to a distillation tower vacuum pump;

[0009] The reaction system 2 includes an R201 reactor, an R202 reactor, and an R203 reactor which are connected in series in sequence, and are all connected to a condenser. The condenser is respectively connected to the distillation tower 3 and the reactor vacuum pump. The R201 output pump is respectively connected to the R201 reactor, the R202 reactor, the R203 reactor, and the reaction system 1. The R202 output pump is respectively connected to the strip making and packaging system 2, the R202 reactor, and the R203 reactor. The R203 output pump is respectively connected to the R203 reactor and the strip making and packaging system 1. The heat medium in the R203 reactor is molten salt, the heat medium in the R201 reactor is heat transfer oil, the heat medium in the R202 reactor is heat transfer oil, and the refrigerant is ethylene tar from the distillation tower 1. The heat medium in the reaction system 1 is molten salt.

[0010] Furthermore, the distillation tower two includes a distillation tower body two, the distillation tower body two, the second tower circulation pump, and the second tower reboiler are connected in a circular manner, the second tower evaporator and the second tower reboiler are connected in parallel, the distillation tower body two is connected to the second tower delivery pump, and the second tower delivery pump is respectively connected to the distillation tower three, the reaction system two, the reaction system one, and the strip making and packaging system two, the distillation tower body two, the second tower heat exchanger, the second tower condenser, the second tower reflux tank, and the second tower reflux pump are connected in a circular manner, the second tower condenser and the second tower reflux tank are respectively connected to the distillation tower vacuum pump, the distillation tower body two is connected to the second tower preheater, and the second tower delivery pump is respectively connected to the R201 reactor and the R202 reactor.

[0011] Furthermore, the distillation tower three includes a distillation tower body three, the distillation tower body three, the three-tower circulation pump, and the three-tower reboiler are connected in a circular manner, the three-tower evaporator and the three-tower reboiler are connected in parallel, the distillation tower body three is connected to the three-tower delivery pump, and the three-tower delivery pump is respectively connected to the reaction system one, the reaction system two, and the strip making and packaging system two, the distillation tower body three, the three-tower preheater, and the distillation tower two are connected in sequence, the distillation tower body three, the three-tower heat exchanger, the three-tower condenser, the three-tower reflux tank, and the three-tower reflux pump are connected in a circular manner, the oil receiving tank is respectively connected to the three-tower reflux pump, the light oil condenser, the midship delivery pump, the reaction system one, and the reaction system two, the three-tower reflux tank and the three-tower heat exchanger are respectively connected to the distillation tower vacuum pump, the three-tower delivery pump is respectively connected to the R201 reactor and the R202 reactor, and the oil receiving tank is connected to the condenser of the reaction system two.

[0012] Furthermore, the reaction system 1 includes an R101 reactor, an R101 delivery pump, an R102 reactor, and an R102 delivery pump connected in sequence, the R101 condenser is respectively connected to the R101 reactor and the R102 reactor, the R102 condenser is respectively connected to the R101 reactor and the R102 reactor, the R101 condenser and the R102 condenser are respectively connected to the reactor vacuum pump, the R101 condenser and the R102 condenser are both connected to the distillation tower 3, and the R201 reactor is connected to the R101 reactor through the R201 output pump.

[0013] Furthermore, the strip making and packaging system includes a strip making machine, a silo, and a packaging machine which are connected in sequence.

[0014] Furthermore, the strip making and packaging system 2 includes a strip making machine 2, a silo 2, and a packaging machine 2 which are connected in sequence.

[0015] A continuous high softening point spinnable asphalt processing method comprises the following steps:

[0016] S1. Ethylene tar is preheated to 200-240℃ in multiple stages and then enters the middle and upper part of the distillation tower body. It is evenly distributed by the distributor in the tower and subjected to vacuum distillation at a vacuum degree of 10-25kPa and a temperature of 200-240℃. After some low-boiling point components are vaporized, they are heat-exchanged in a heat exchanger at the light component outlet at the top of the tower, and the gas phase is converted into a liquid phase, which is collected in a tower reflux tank as the tower top product. A part of it is refluxed, and the gas-liquid reflux forms a countercurrent contact between gas and liquid phases on the surface of the packing, thereby obtaining a relatively pure light component product at the top of the tower; a part of it is extracted to the finished product tank area as catalytic hydrogenation diesel feedstock oil;

[0017] S2. The unvaporized heavy components enter the bottom of the second distillation tower body and are preheated to 270-280°C by the second tower delivery pump before entering the middle and upper part of the second distillation tower body. They are evenly distributed by the distributor in the tower and are subjected to vacuum distillation at a vacuum degree of 10-25kPa and a temperature of 280-330°C. After some low-boiling point components are vaporized, they are converted from the light component outlet at the top of the tower to the liquid phase after heat exchange by the second tower heat exchanger. The gas phase is collected in the first tower reflux tank as the tower top product, and part of them are refluxed. The gas-liquid reflux forms a countercurrent contact between the gas and liquid phases on the surface of the packing, thereby obtaining a relatively pure light component product at the top of the tower; part of them are extracted to the finished product tank area as catalytic hydrogenation diesel feedstock oil; the tower top reflux tank has the function of cutting water and separating oil, and can cut off part of the water content of the tower top product;

[0018] S3. The unvaporized heavy components enter the bottom of the second distillation tower body, and are transported to the second tower reboiler and the second tower evaporator through the second tower circulation pump, and enter the upper part of the stripping section tower plate. The kinetic energy of the rising gas phase is used to push the heavy components forward, and the gas and liquid phases flow in the same direction on the tower plate, reducing the liquid level difference, while 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 further heating and evaporation separation, the sample is sampled and tested from the sampling port of the sampler after staying for 1-20 hours. After the tower bottom product is qualified, asphalt with a softening point of 100-150℃ can be produced;

[0019] S4. The asphalt in step S2 is preheated to 250-310°C in the three-tower preheater and then enters the distillation tower body 3. The principle of the distillation tower body 3 is similar to that of the distillation tower body 1, but the processing capacity is reduced. The top of the distillation tower body 3 produces marine fuel oil, and the bottom of the tower produces asphalt with a softening point of 120-180°C;

[0020] S5. The bottom product of step S3 is pumped to the R101 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree of 5-20 kPa and temperature of 300-375 ° C to obtain asphalt with a softening point of 150-200 ° C. The light component produced is cooled, collected and sent to the finished product tank area for storage as marine fuel oil;

[0021] S6. The asphalt obtained in step S3 is pumped to the R102 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree of 5-20 kPa and temperature of 300-375°C to obtain asphalt with a softening point of 180-220°C. The light components produced are cooled, collected and sent to the finished product tank area for storage as marine fuel oil;

[0022] S7. The bottom product obtained in step S2 is sent to the R201 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under the conditions of vacuum degree 5-20kPa and temperature 300-375°C to obtain asphalt with a softening point of 150-200°C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0023] S8. The bottom product obtained in step S2 is sent to the R202 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree of 5-20 kPa and temperature of 300-375 ° C to obtain asphalt with a softening point of 150-200 ° C. The light component produced is cooled, collected and sent to the finished product tank area for storage as marine fuel oil;

[0024] S9. The bottom product obtained in step S7 is sent to the R101 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under the conditions of vacuum degree 5-20kPa and temperature 300-375°C to obtain asphalt with a softening point of 150-200°C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0025] S10. The bottom product obtained in step S7 is sent to the R202 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under the conditions of vacuum degree 5-20kPa and temperature 300-375°C to obtain asphalt with a softening point of 150-200°C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0026] S11. The bottom product obtained in step S10 is sent to the R203 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20kPa and temperature 300-375°C to obtain asphalt with a softening point of 200-250°C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0027] S12. The bottom product obtained in step S9 is sent to the R102 reactor for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375 ° C to obtain asphalt with a softening point of 200-250 ° C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0028] S13. The asphalt with a softening point of 200-250° C. obtained in step S12 is cooled, granulated, transported and packaged and then stored in a finished product warehouse.

[0029] The utility model achieves the cutting of product distillation range under different working conditions. By adding a distillation tower to perform preliminary light and heavy component separation of ethylene tar, the problem of excessive gas phase load at the top of the tower is completely solved. The processing capacity is increased by more than 60% on the basis of the original technology. At the same time, the distillation tower can cut out important components of the negative electrode liquid phase coating agent of the lithium battery to increase the product variety. Using ternary molten salt, the reaction temperature and residence time are controlled through the process. A set of reaction systems is added, which includes three reactors. The three reactors can be connected in series to the reactors in the original technology, so that the process can achieve the purpose of increasing the reaction residence time, and then the product can be more fully subjected to thermal polycondensation reaction. Without using a short-range molecular distiller, a product with a higher softening point and a higher coking value can be produced. Through continuous production, a 200-250℃ negative electrode coating asphalt with a narrower distribution of asphalt components and more stable quality can be produced. Through the series and parallel connection of the tower and the reactor, the processing volume can be increased under the premise of low energy consumption, and multiple production lines can simultaneously produce high softening point spinnable asphalt. In view of the structure of the distillation tower and the reactor, a higher coking value of the pitch at the same softening point can be achieved. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 It is a schematic diagram of the utility model.

[0031] Among them: 1. Preheater of tower 1; 2. Reboiler of tower 1; 3. Condenser of tower 1; 4. Distillation tower body 1; 5. Reflux tank of tower 1; 6. Reflux pump of tower 1; 7. Circulation pump of tower 1; 8. Delivery pump of tower 1; 9. Preheater of tower 2; 10. Evaporator of tower 2; 11. Reboiler of tower 2; 12. Circulation pump of tower 2; 13. Distillation tower body 2; 14. Heat exchanger of tower 2; 15. Condenser of tower 2; 16. Reflux tank of tower 2; 17. Reflux pump of tower 2; 18. Delivery pump of tower 2; 19. Evaporator of tower 3; 20. Reboiler of tower 3; 21. Circulation pump of tower 3; 22. Preheater of tower 3; 23. Distillation tower body 3; 24. Reflux pump of tower 3; 25. Reflux tank of tower 3; 26. Heat exchanger of tower 3; 27. Condenser of tower 3 ; 28. Oil receiving tank; 29. ​​Three-tower delivery pump; 30. China Ship delivery pump; 31. Distillation tower vacuum pump; 32. Light oil condenser; 33. R101 reactor; 34. R102 reactor; 35. R101 delivery pump; 36. R102 delivery pump; 37. R101 condenser; 38. R102 condenser; 39. Reactor vacuum pump; 40. R201 reactor; 41. R202 reactor; 42. R203 reactor; 43. R201 output pump; 44. R202 output pump; 45. R203 output pump; 46. Strip making machine one; 47. Silo one; 48. Packaging machine one; 49. Strip making machine two; 50. Silo two; 51. Packaging machine two. DETAILED DESCRIPTION

[0032] The following is combined with Figure 1 The specific implementation methods of the utility model are further described.

[0033] A continuous production device for high-softening-point spinnable asphalt comprises a distillation tower 1, a distillation tower 2 and a distillation tower 3 which are connected in series in sequence and are respectively connected to a distillation tower vacuum pump 31; a reaction system 1 is respectively connected to the distillation tower 2 and the distillation tower 3; the reaction system 2 is connected in series / in parallel with the reaction system 1; the reaction system 2 is connected to the distillation tower 2; the reaction system 1 and the reaction system 2 are both connected to a strip making and packaging system 1; the distillation tower 2 and the distillation tower 3 are both connected to a strip making and packaging system 2.

[0034] The distillation tower one includes a distillation tower body one 4, the distillation tower body one 4 is connected to a tower preheater 1, the tower preheater 1 is connected to a distillation tower two, the distillation tower body one 4, a tower circulation pump 7, and a tower reboiler 2 are connected in a circular manner, the distillation tower body one 4, a tower delivery pump 8, a tower preheater 9, and a distillation tower two are connected in a circular manner, the distillation tower body one 4, a tower condenser 3, a tower reflux tank 5, and a tower reflux pump 6 are connected in a circular manner, and the tower reflux tank 5 is connected to the distillation tower vacuum pump 31.

[0035] The reaction system 2 includes an R201 reactor 40, an R202 reactor 41, and an R203 reactor 42 which are connected in series in sequence, and are all connected to a condenser. The condenser is respectively connected to the distillation tower 3 and the reactor vacuum pump 39. The R201 output pump 43 is respectively connected to the R201 reactor 40, the R202 reactor 41, the R203 reactor 42, and the reaction system 1. The R202 output pump 44 is respectively connected to the strip making and packaging system 2, the R202 reactor 41, and the R203 reactor 42. The R203 output pump 45 is respectively connected to the R203 reactor 42 and the strip making and packaging system 1. The heat medium in the R203 reactor 42 is molten salt, the heat medium in the R201 reactor 40 is heat transfer oil, the heat medium in the R202 reactor 41 is heat transfer oil, and the refrigerant is ethylene tar from the distillation tower 1. The heat medium in the reaction system 1 is molten salt.

[0036] The distillation tower two includes a distillation tower body two 13, the distillation tower body two 13, a second tower circulation pump 12, and a second tower reboiler 11 are connected in a circular manner, the second tower evaporator 10 is connected in parallel with the second tower reboiler 11, the distillation tower body two 13 is connected with the second tower delivery pump 18, and the second tower delivery pump 18 is respectively connected with the distillation tower three, the reaction system two, the reaction system one, and the strip making and packaging system two, the distillation tower body two 13, the second tower heat exchanger 14, the second tower condenser 15, the second tower reflux tank 16, and the second tower reflux pump 17 are connected in a circular manner, the second tower condenser 15 and the second tower reflux tank 16 are respectively connected with the distillation tower vacuum pump 31, the distillation tower body two 13 is connected with the second tower preheater 9, and the second tower delivery pump 18 is respectively connected with the R201 reactor 40 and the R202 reactor 41.

[0037] The distillation tower three includes a distillation tower body three 23, the distillation tower body three 23, the three-tower circulation pump 21, and the three-tower reboiler 20 are connected in a circular manner in sequence, the three-tower evaporator 19 is connected in parallel with the three-tower reboiler 20, the distillation tower body three 23 is connected with the three-tower delivery pump 29, and the three-tower delivery pump 29 is respectively connected with the reaction system one, the reaction system two, and the strip packaging system two, the distillation tower body three 23, the three-tower preheater 22, and the distillation tower two are connected in sequence, the distillation tower body three 23, the three-tower heat exchanger 26, and the three-tower The condenser 27, the three-tower reflux tank 25, and the three-tower reflux pump 24 are connected in a circular manner in sequence, the oil receiving tank 28 is respectively connected to the three-tower reflux pump 24, the light oil condenser 32, the midship transfer pump 30, the reaction system one, and the reaction system two, the three-tower reflux tank 25 and the three-tower heat exchanger 26 are respectively connected to the distillation tower vacuum pump 31, the three-tower transfer pump 29 is respectively connected to the R201 reactor 40 and the R202 reactor 41, and the oil receiving tank 28 is connected to the condenser of the reaction system two.

[0038] The reaction system 1 includes an R101 reactor 33, an R101 delivery pump 35, an R102 reactor 34, and an R102 delivery pump 36 connected in sequence. The R101 condenser 37 is connected to the R101 reactor 33 and the R102 reactor 34 respectively. The R102 condenser 38 is connected to the R101 reactor 33 and the R102 reactor 34 respectively. The R101 condenser 37 and the R102 condenser 38 are connected to the reactor vacuum pump 39 respectively. The R101 condenser 37 and the R102 condenser 38 are both connected to the distillation tower 3. The R201 reactor 40 is connected to the R101 reactor 33 through the R201 output pump 43.

[0039] The strip making and packaging system comprises a strip making machine 46, a silo 47, and a packaging machine 48 which are connected in sequence.

[0040] The strip making and packaging system 2 comprises a strip making machine 2 49, a silo 2 50, and a packaging machine 2 51 which are connected in sequence.

[0041] A continuous high softening point spinnable asphalt processing method comprises the following steps:

[0042] S1. Ethylene tar is preheated to 200-240℃ in multiple stages and then enters the middle and upper part of the distillation tower body 4. It is evenly distributed by the distributor in the tower and subjected to vacuum distillation at a vacuum degree of 10-25kPa and a temperature of 200-240℃. After some low-boiling point components are vaporized, they are heat-exchanged in a heat exchanger at the light component outlet at the top of the tower, and the gas phase is converted into a liquid phase, which is collected in a tower reflux tank 5 as a tower top product. A part of it is refluxed, and the gas-liquid reflux forms a gas-liquid two-phase countercurrent contact on the surface of the packing, thereby obtaining a relatively pure light component product at the top of the tower; a part of it is extracted to the finished product tank area as catalytic hydrogenation diesel feedstock oil;

[0043] S2. The unvaporized heavy components enter the bottom of the second distillation tower body 13 and are preheated to 270-280°C by the second tower delivery pump 18 before entering the middle and upper part of the second distillation tower body 13. They are evenly distributed by the distributor in the tower and are subjected to vacuum distillation at a vacuum degree of 10-25kPa and a temperature of 280-330°C. After some low-boiling point components are vaporized, they are converted from the light component outlet at the top of the tower to the liquid phase after heat exchange by the second tower heat exchanger 14 and collected in the first tower reflux tank 5 as the top product. A part of them is refluxed, and the gas-liquid reflux forms a countercurrent contact between the gas and liquid phases on the surface of the packing, thereby obtaining a relatively pure light component product at the top of the tower; a part of them is extracted to the finished product tank area as catalytic hydrogenation diesel feedstock oil; the top reflux tank has the function of cutting water and separating oil, and can cut off part of the water content of the top product;

[0044] S3. The unvaporized heavy components enter the bottom of the second distillation tower body 13, and are transported to the second tower reboiler 11 and the second tower evaporator 10 through the second tower circulation pump 12, and enter the upper part of the stripping section tower plate, and use the kinetic energy of the rising gas phase to push the heavy components forward, and make the gas and liquid phases flow in the same direction on the tower plate, reduce the liquid level difference, and at the same time increase the gas flow speed and distribution points, increase the liquid surface area, and increase the probability of light components escaping. After further heating and evaporation separation, the sample is sampled and tested from the sampling port of the sampler after staying for 1-20 hours. After the tower bottom product is qualified, asphalt with a softening point of 100-150℃ can be produced;

[0045] S4. The asphalt in step S2 is preheated to 250-310°C by the three-tower preheater 22 and then enters the distillation tower body 3 23. The principle of the distillation tower body 3 23 is similar to that of the distillation tower body 1 4, but the processing capacity is reduced. The top of the distillation tower body 3 23 produces marine fuel oil, and the bottom of the tower produces asphalt with a softening point of 120-180°C;

[0046] S5. The bottom product of step S3 is pumped to R101 reactor 33 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375 ° C to obtain asphalt with a softening point of 150-200 ° C. The light component produced is cooled, collected and sent to the finished product tank area for storage as marine fuel oil;

[0047] S6. The asphalt obtained in step S3 is pumped to the R102 reactor 34 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375 ° C to obtain asphalt with a softening point of 180-220 ° C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0048] S7. The bottom product obtained in step S2 is sent to R201 reactor 40 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375° C. to obtain asphalt with a softening point of 150-200° C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0049] S8. The bottom product obtained in step S2 is sent to R202 reactor 41 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375 ° C to obtain asphalt with a softening point of 150-200 ° C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0050] S9. The bottom product obtained in step S7 is sent to R101 reactor 33 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375°C to obtain asphalt with a softening point of 150-200°C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0051] S10. The bottom product obtained in step S7 is sent to R202 reactor 41 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375 ° C to obtain asphalt with a softening point of 150-200 ° C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0052] S11. The bottom product obtained in step S10 is sent to R203 reactor 42 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375°C to obtain asphalt with a softening point of 200-250°C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0053] S12. The bottom product obtained in step S9 is sent to R102 reactor 34 for stirring and heat polycondensation reaction. The reaction is carried out for 1-10 hours under vacuum degree 5-20 kPa and temperature 300-375 ° C to obtain asphalt with a softening point of 200-250 ° C. The light component produced is collected after cooling and sent to the finished product tank area for storage as marine fuel oil;

[0054] S13. The asphalt with a softening point of 200-250° C. obtained in step S12 is cooled, granulated, transported and packaged and then stored in a finished product warehouse.

[0055] Each reactor is slender, with a length-to-diameter ratio of 1:2-1:3, and its agitator blades are straight structures to reduce asphalt backmixing in the reactor.

[0056] The heating medium for each distillation tower body and reactor jacket can be heat transfer oil and 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 complicated to operate.

[0057] Distillation tower 2, distillation tower 3, R101 reactor 33, R102 reactor 34, R201 reactor 40, and R202 reactor 41 are connected by cross-lines, so that different process combinations can be realized, such as two towers and two reactors, two towers and three reactors, three towers and two reactors, and three processes. The combination of different processes can meet the user's requirements for different coated asphalts.

[0058] Ethylene tar first exchanges heat with the light component steam at the top of the distillation tower body three 23, passes through the three-tower preheater 22, then passes through the second tower preheater 9, and then passes through the first tower preheater 1 to enter the distillation tower body one 4, and separates the light and heavy components (negative pressure operation). The light component gas flows out from the top of the tower after passing through the distillation section, and enters the first tower reflux tank 5 after being cooled by the tower top cooler. It is divided into two parts after passing through the pump and the flow meter after the pump. One part of the reflux is sent back to the top of the tower for reflux, and the remaining light fuel oil is sent to the finished product tank area (light fuel oil storage tank). After removing the light component, the rest enters the bottom of the tower, and the heavy component is transported to the second tower preheater 9 by the asphalt delivery pump for heating and then enters the distillation tower body two 13. The light component gas flows out from the top of the tower after passing through the distillation section, and enters the second tower reflux tank 16 after being cooled by the second tower preheater 9 tower top cooler and the second tower condenser 15. It is divided into two parts by the pump, one part is refluxed back to the top of the tower for reflux, and the remaining light fuel oil is sent to the finished product tank area. The heavy component part of the distillation tower body 2 13 is transported into the second tower reboiler 11 and the second tower evaporator 10 for further heating through the second tower circulation pump 12, and then returns to the bottom and middle of the tower. The qualified asphalt is transported by the second tower delivery pump 18: one part is transported to the granulator for direct granulation to produce coated asphalt with a softening point of 120℃, and one part enters the distillation tower body 3 23 for further separation of light and heavy components. The light component part of the top of the tower is heat exchanged with the raw oil and enters the oil receiving tank 28, and is pumped to the medium-quality fuel oil storage tank by the output pump; the heavy component part at the bottom of the tower enters the reactor for thermal polycondensation reaction.

[0059] The product from the second distillation tower body 13 can be selectively sent to the R201 reactor 40 or the R101 reactor 33 by the second tower delivery pump 18. The qualified 150-180℃ coated asphalt sent to the R101 reactor 33 after thermal polymerization can be sent to the granulator by the R101 delivery pump 35 for granulation and packaging, or sent to the R102 reactor 34 for further thermal polymerization to produce 180-200℃ coated asphalt. The heavy components in the product sent to the R201 reactor 40 can be selectively sent to the R202 reactor 41 or the R101 reactor 33 after thermal polymerization. The product sent to the R202 reactor 41 can be sent to the R202 output pump 44 to produce 180-200℃ coated asphalt, or sent to the R203 reactor 42 to produce 200-250℃ coated asphalt.

[0060] Thermal oil:

[0061] The heat transfer oil in the utility model adopts hydrogenated terphenyls, English name: Hydrogenated terphenyls, CAS number: 61788-32-7, and the main component is a mixture of partially hydrogenated terphenyl isomers. Hydrogenated terphenyl is a high-temperature synthetic heat transfer oil with excellent thermal stability, oxidation resistance and low vapor pressure.

[0062] Excellent thermal stability, liquid phase operation at 345℃. Antioxidation, hydrogenated terphenyl is protected against oxidation by an expansion tank (with pressure protection, nitrogen addition, and liquid seal inside), without adding antioxidants, which also enhances its thermal stability. Even when hydrogenated terphenyl is used at 345℃, the vapor pressure is only 75.4kpa, and it can be pumped at temperatures below -32℃. Therefore, hydrogenated terphenyl is the best choice under conditions that require both low-temperature and high-temperature capabilities. Non-corrosive to equipment. Non-corrosive to iron and non-ferrous metal materials used in general industrial devices. Good viscosity-temperature performance, low viscosity at room temperature, and good pumpability. It can be used for a long time within the allowable range of temperature indicators and can be regenerated.

[0063] Molten salt:

[0064] The molten salt in the utility model adopts ternary molten salt, which is a mixed nitrate composed of 53% potassium nitrate + 40% sodium nitrite + 7% sodium nitrate, and has a melting point of 142 degrees Celsius and a vaporization point of 500 degrees Celsius. Sodium nitrite will slowly decompose above 450 degrees Celsius. The molten salt does not require a supporting electrolyte like an aqueous solution, and has the characteristics of an ionic melt, a wide range of operating temperature, low vapor pressure, volume heat capacity, large latent heat of phase change, high solubility, low viscosity, stable physical and chemical properties, and a large decomposition voltage.

[0065] The following is the comparison data between the utility model and the existing process:

[0066]

[0067] The above is only a preferred specific implementation method of the utility model, but the protection scope of the utility model is not limited to this. Any technician familiar with the technical field within the technical scope disclosed by the utility model, according to the technical scheme and utility model concept of the utility model, shall be covered by the protection scope of the utility model.

Claims

1. A continuous production device for high softening point spinnable asphalt, characterized in that: It comprises a distillation tower 1, a distillation tower 2 and a distillation tower 3 which are connected in series in sequence and are respectively connected to a distillation tower vacuum pump (31); a reaction system 1 is respectively connected to the distillation tower 2 and the distillation tower 3; the reaction system 2 is connected in series / in parallel with the reaction system 1; the reaction system 2 is connected to the distillation tower 2; the reaction system 1 and the reaction system 2 are both connected to a strip making and packaging system 1; the distillation tower 2 and the distillation tower 3 are both connected to a strip making and packaging system 2; The first distillation tower comprises a first distillation tower body (4), the first distillation tower body (4) is connected to a first tower preheater (1), the first tower preheater (1) is connected to a second distillation tower, the first distillation tower body (4), a first tower circulation pump (7), and a first tower reboiler (2) are connected in a circular manner, the first distillation tower body (4), a first tower delivery pump (8), a second tower preheater (9), and the second distillation tower are connected in a circular manner, the first distillation tower body (4), a first tower condenser (3), a first tower reflux tank (5), and a first tower reflux pump (6) are connected in a circular manner, and the first tower reflux tank (5) is connected to a distillation tower vacuum pump (31); The reaction system 2 comprises an R201 reactor (40), an R202 reactor (41), and an R203 reactor (42) which are connected in series in sequence, and each of them is connected to a condenser. The condenser is connected to the distillation tower 3 and the reactor vacuum pump (39), respectively. The R201 output pump (43) is connected to the R201 reactor (40), the R202 reactor (41), the R203 reactor (42), and the reaction system 1, respectively. The R202 output pump (44) is connected to the R201 reactor (40), the R202 reactor (41), the R203 reactor (42), and the reaction system 1, respectively. The strip packaging system 2, the R202 reactor (41), and the R203 reactor (42) are connected, and the R203 output pump (45) is respectively connected to the R203 reactor (42) and the strip packaging system 1; the heat medium in the R203 reactor (42) is molten salt, the heat medium in the R201 reactor (40) is heat transfer oil, the heat medium in the R202 reactor (41) is heat transfer oil, and the cooling medium is ethylene tar from the distillation tower 1; the heat medium in the reaction system 1 is molten salt.

2. The continuous high softening point spinnable asphalt production device according to claim 1 is characterized in that: The distillation tower 2 comprises a distillation tower body 2 (13), wherein the distillation tower body 2 (13), a second tower circulation pump (12), and a second tower reboiler (11) are sequentially connected in a circular manner, the second tower evaporator (10) and the second tower reboiler (11) are connected in parallel, the distillation tower body 2 (13) is connected to a second tower delivery pump (18), and the second tower delivery pump (18) is respectively connected to the distillation tower 3, the reaction system 2, the reaction system 1, and the strip making and packaging system 2, the distillation tower body 2 ( 13), the second tower heat exchanger (14), the second tower condenser (15), the second tower reflux tank (16), and the second tower reflux pump (17) are connected in a circular manner in sequence; the second tower condenser (15) and the second tower reflux tank (16) are respectively connected to the distillation tower vacuum pump (31); the distillation tower body (13) is connected to the second tower preheater (9); and the second tower delivery pump (18) is respectively connected to the R201 reactor (40) and the R202 reactor (41).

3. The continuous high softening point spinnable asphalt production device according to claim 1, characterized in that: The distillation tower three comprises a distillation tower body three (23), the distillation tower body three (23), a three-tower circulation pump (21), and a three-tower reboiler (20) are connected in a circular manner in sequence, the three-tower evaporator (19) and the three-tower reboiler (20) are connected in parallel, the distillation tower body three (23) is connected to a three-tower delivery pump (29), and the three-tower delivery pump (29) is respectively connected to the reaction system one, the reaction system two, and the strip making and packaging system two, the distillation tower body three (23), the three-tower preheater (22), and the distillation tower two are connected in sequence, the distillation tower body three (23), the three-tower heat exchanger (26), and the three-tower heat exchanger (27) are connected in parallel, and the three-tower heat exchanger (27) is connected in parallel. The tower condenser (27), the three-tower reflux tank (25), and the three-tower reflux pump (24) are connected in a circular manner in sequence; the oil receiving tank (28) is respectively connected to the three-tower reflux pump (24), the light oil condenser (32), the midship transfer pump (30), the reaction system 1, and the reaction system 2; the three-tower reflux tank (25) and the three-tower heat exchanger (26) are respectively connected to the distillation tower vacuum pump (31); the three-tower transfer pump (29) is respectively connected to the R201 reactor (40) and the R202 reactor (41); and the oil receiving tank (28) is connected to the condenser of the reaction system 2.

4. The continuous high softening point spinnable asphalt production device according to claim 1 is characterized in that: The reaction system 1 comprises an R101 reactor (33), an R101 delivery pump (35), an R102 reactor (34), and an R102 delivery pump (36) which are connected in sequence; an R101 condenser (37) is connected to the R101 reactor (33) and the R102 reactor (34) respectively; an R102 condenser (38) is connected to the R101 reactor (33) and the R102 reactor (34) respectively; the R101 condenser (37) and the R102 condenser (38) are connected to the reactor vacuum pump (39) respectively; the R101 condenser (37) and the R102 condenser (38) are both connected to the distillation tower 3; and an R201 reactor (40) is connected to the R101 reactor (33) via an R201 delivery pump (43).

5. The continuous high softening point spinnable asphalt production device according to claim 1, characterized in that: The strip making and packaging system 1 comprises a strip making machine 1 (46), a material bin 1 (47), and a packaging machine 1 (48) which are connected in sequence.

6. The continuous high softening point spinnable asphalt production device according to claim 1, characterized in that: The strip making and packaging system 2 comprises a strip making machine 2 (49), a material bin 2 (50), and a packaging machine 2 (51) which are connected in sequence.

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