CN111961495A

CN111961495A - Production process and system for modifying asphalt by multi-kettle series-connected tubular furnace heating method

Info

Publication number: CN111961495A
Application number: CN202010919712.9A
Authority: CN
Inventors: 杨雪松
Original assignee: Acre Coking and Refractory Engineering Consulting Corp MCC
Current assignee: Acre Coking and Refractory Engineering Consulting Corp MCC
Priority date: 2020-09-04
Filing date: 2020-09-04
Publication date: 2020-11-20

Abstract

The invention relates to a production process and a system for modified asphalt by a multi-kettle series-connected tubular furnace heating method, wherein the production process for the modified asphalt is a single-furnace single-kettle stripping flash evaporation process and comprises a primary modification reaction process; or the production process of the modified asphalt is a double-furnace double-kettle stripping flash evaporation process, which comprises a primary modification reaction process and a secondary modification reaction process; in the single modification reaction process, more than 2 reaction kettles are adopted for series operation. The invention can effectively improve the treatment capacity of single modification reaction, further improve the production capacity of a single production line and meet the matching requirement of the existing tar device.

Description

Production process and system for modifying asphalt by multi-kettle series-connected tubular furnace heating method

Technical Field

The invention relates to the technical field of modified asphalt production, in particular to a production process and a system for modified asphalt by a multi-kettle series-connected tubular furnace heating method.

Background

About 50% -60% of asphalt is generally generated in the coal tar processing process, which belongs to a bulk product of tar processing, and the larger the processing scale is, the more the asphalt yield is. The modified asphalt is the main downstream product of the existing asphalt and is mainly used for producing prebaked anodes in the electrolytic aluminum industry to prepare battery rods or electrode binders.

At present, the production process for producing modified asphalt in China mostly adopts a thermal polycondensation method, which can be divided into a kettle type heating method and a tube furnace heating method according to the heating mode. The production process of modified asphalt by tubular furnace heating method includes pressurized double-furnace double-kettle stripping flash evaporation process introduced from France, domestic normal-pressure or reduced-pressure double-furnace double-kettle stripping flash evaporation process, single-furnace single-kettle stripping flash evaporation process, etc.

The double-furnace double-kettle stripping flash evaporation process takes medium-temperature asphalt as a raw material, the asphalt is heated by a tubular heating furnace, and then modification reaction is carried out in a reaction kettle; the modification reaction is divided into a first modification reaction and a second modification reaction, and the two modification reactions can be normal pressure reaction, pressure reaction or pressure reduction reaction according to different requirements of products, and the modified asphalt product is obtained by flash evaporation and steam stripping of a stripping tower after the reaction. The double-furnace double-kettle stripping flash evaporation process has the advantages that two steps of reactions are adopted, the reaction temperature and the reaction time of each step are different, the purpose of the reaction is different, the generation amount of alpha-components and beta-components can be effectively controlled, and the product quality is controllable; in addition, the method for separating asphalt and oil products by adopting a stripping method is favorable for adjusting the softening point.

The Chinese patent application with the application publication number of CN 110240918A discloses a system and a process for producing modified asphalt by double-furnace double-kettle stripping flash evaporation, wherein the system comprises a 1# reaction kettle, a 1# full-flow buffer tank, a 1# tubular furnace, a first asphalt circulation loop, a 2# reaction kettle, a 2# full-flow buffer tank, a 2# tubular furnace and a second asphalt circulation loop; flexible baffles are respectively arranged in the No. 1 reaction kettle and the No. 2 reaction kettle, and a No. 1 full flow buffer tank is arranged on the first asphalt circulating loop; and a No. 2 full flow buffer tank is arranged on the second asphalt circulating loop. In the invention, the side feeding and bottom discharging mode of the reaction kettle is changed into a side feeding and full flow discharging mode, the full flow buffer tank is arranged behind the reaction kettle, the outflow of the reaction kettle is controlled by maintaining the stable asphalt liquid level in the full flow buffer tank, the accurate control of the reaction residence time is finally realized by controlling the liquid level in the reaction kettle to be constant, and the production process of the modified asphalt can be carried out for a long time and smoothly.

The single-furnace single-kettle stripping flash evaporation process also takes medium-temperature asphalt as a raw material, asphalt is heated in a tubular heating furnace, then the asphalt is reacted in a reaction kettle, and the modified asphalt is obtained by flash stripping in a stripping tower after the reaction; because the reaction is completed in one step, the product quality control of the single-furnace single-kettle stripping flash process is not flexible as the double-furnace double-kettle stripping flash process.

The modified asphalt production process by the tubular furnace heating method achieves the aim of asphalt modification according to the residence time and the reaction temperature of reactants of medium-temperature asphalt in a modified asphalt reaction kettle, the residence time is realized by controlling the volume of the reaction kettle, and the reaction temperature is ensured by a tubular heating furnace.

With the continuous increase of the single set of treatment capacity of the tar device (15 ten thousand t/a or 20 ten thousand t/a in the past, and 30 ten thousand t/a or 50 ten thousand t/a in the present), the traditional double-furnace double-kettle modified asphalt production process cannot meet the requirements only by a single production line, and the volume of the reaction kettle cannot be infinitely increased due to the retention time, so that the production of the modified asphalt by the tar processing device with 30 ten thousand t/a or 50 ten thousand t/a in the present stage is often required to be matched with two or even a plurality of modified asphalt production lines.

Two or even a plurality of modified asphalt production lines are adopted, so that the occupied area is large, the control system is complex, the number of operators is large, and the production cost is high; if a production line is adopted, a plurality of reaction kettles are arranged in each step of reaction process for parallel operation, and the problems can be solved by corresponding control process.

In summary, it is very necessary to improve the production process of the double-furnace double-kettle modified asphalt by the conventional tubular furnace heating method, and to increase the throughput of a single production line by parallel operation of a plurality of modified asphalt reaction kettles.

Disclosure of Invention

The invention provides a multi-kettle series tubular furnace heating method modified asphalt production process and system, wherein two or more reaction kettles are arranged for series operation in a single modification reaction process, so that the treatment capacity of the single modification reaction can be effectively improved, the production capacity of a single production line is further improved, and the matching requirements of the existing tar device are met.

In order to achieve the purpose, the invention adopts the following technical scheme:

the production process of the modified asphalt by a tubular furnace heating method with a plurality of serially connected reaction kettles is a single-furnace single-kettle stripping flash evaporation process and comprises a primary modification reaction process; or the production process of the modified asphalt is a double-furnace double-kettle stripping flash evaporation process, which comprises a primary modification reaction process and a secondary modification reaction process; in the single modification reaction process, more than 2 reaction kettles are adopted for series operation.

The modified asphalt production process is a normal-pressure double-furnace double-kettle stripping flash evaporation process, wherein the double kettles are a 1# reaction kettle group and a 2# reaction kettle group, the 1# reaction kettle group is formed by connecting a 1# reaction kettle A and a 1# reaction kettle B in series, and the 2# reaction kettle group is formed by connecting a 2# reaction kettle A and a 2# reaction kettle B in series.

The production process of the modified asphalt by a tubular furnace heating method with multiple serially connected reaction kettles specifically comprises the following steps:

1) mixing raw material medium-temperature asphalt with outlet asphalt of a No. 1 tubular furnace, and then sequentially entering a No. 1 reaction kettle A and a No. 1 reaction kettle B for primary modification reaction; during the primary modification reaction, the temperature in the 1# reaction kettle A and the 1# reaction kettle B is controlled to be 360-400 ℃, the asphalt is mainly subjected to beta-modification reaction, and flash evaporation oil gas generated by flash evaporation cracking is discharged into an external stripping tower through a flash evaporation oil gas outlet at the top of the corresponding reaction kettle; the asphalt in the No. 1 reaction kettle A enters the No. 1 reaction kettle B, and primary modification reaction is completed in the No. 1 reaction kettle B;

2) most of the asphalt after the primary modification reaction is used as circulating asphalt, the circulating asphalt is sent to a No. 1 tubular furnace for heating through a No. 1 asphalt circulating pump, then the circulating asphalt flows back to a No. 1 reaction kettle A and a No. 1 reaction kettle B to be used as heat sources, and the residual asphalt flows into a No. 1 full-flow buffer tank through a full-flow valve I in a full-flow mode;

3) pumping the asphalt subjected to primary modification from the bottom of a No. 1 full-flow buffer tank by a No. 1 asphalt output pump, and sequentially entering a No. 2 reaction kettle A and a No. 2 reaction kettle B through a primary modified asphalt pipeline to perform secondary modification reaction;

4) mixing the primarily modified asphalt with outlet asphalt of a 2# asphalt circulating pump, heating the mixture in a 2# tubular furnace, and refluxing the heated mixture to a 2# reaction kettle A and a 2# reaction kettle B to perform secondary modification reaction; during the secondary modification reaction, the temperature in the 2# reaction kettle A and the 2# reaction kettle B is controlled to be 380-420 ℃, and the asphalt simultaneously carries out alpha-modification reaction and beta-modification reaction; the flash oil gas generated by flash cracking is discharged to an external stripping tower through a flash oil gas outlet at the top of the corresponding reaction kettle; the asphalt in the No. 2 reaction kettle A enters a No. 2 reaction kettle B, and the secondary modification reaction is completed in the No. 2 reaction kettle B;

5) most of the asphalt after the secondary modification is used as circulating asphalt, is sent to a No. 2 tubular furnace for heating through a No. 2 asphalt circulating pump, and then returns to a No. 2 reaction kettle A and a No. 2 reaction kettle B to be used as heat sources; the residual asphalt flows into a No. 2 full-flow buffer tank through a full-flow valve II in a full-flow mode;

6) and pumping the asphalt subjected to secondary modification from the bottom of the 2# full-flow buffer tank by a 2# asphalt output pump, and conveying the asphalt to a stripping tower through a secondary modified asphalt pipeline.

The retention time of the asphalt in the primary modification reaction process is adjusted only by the retention time of the No. 1 reaction kettle B, and the retention time of the asphalt in the No. 1 reaction kettle B is realized in a full flow mode, namely, the retention time is adjusted by setting different full flow heights; the residence time of the asphalt in the secondary upgrading reaction process is adjusted only by the residence time of the 2# reaction kettle B, and the residence time of the asphalt in the 2# reaction kettle B is realized in a full flow mode, namely, the residence time is adjusted by setting different full flow heights.

The raw material medium-temperature asphalt is mixed with outlet asphalt of a No. 1 tubular furnace, enters a No. 1 reaction kettle A from an asphalt inlet at the upper part of the No. 1 reaction kettle A, flows out from an asphalt outlet at the bottom of the No. 1 reaction kettle A, and then enters a No. 1 reaction kettle B from an asphalt inlet at the upper part of the No. 1 reaction kettle B, and an asphalt outlet arranged at the bottom of the No. 1 reaction kettle B is connected with an asphalt full flow pipe I; a plurality of asphalt full-flow ports are formed in the upper edge of the asphalt full-flow pipe I in the height direction, each asphalt full-flow port is connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank through a corresponding asphalt full-flow branch pipe I, and a full-flow valve I is arranged on each asphalt full-flow branch pipe I;

the outlet asphalt of the No. 2 tube furnace enters the No. 2 reaction kettle A from an asphalt inlet at the upper part of the No. 2 reaction kettle A, flows out from an asphalt outlet at the bottom of the No. 2 reaction kettle A, and then enters the No. 2 reaction kettle B from an asphalt inlet at the upper part of the No. 2 reaction kettle B, and an asphalt outlet arranged at the bottom of the No. 2 reaction kettle B is connected with an asphalt full flow pipe II; and a plurality of asphalt full-flow ports are arranged in the upper edge of the asphalt full-flow pipe II in the height direction, each asphalt full-flow port is respectively connected with an asphalt inlet at the top of the 2# full-flow buffer tank through an asphalt full-flow branch pipe II, and a full-flow valve II is respectively arranged on each asphalt full-flow branch pipe II.

After mixing the raw material medium-temperature asphalt with outlet asphalt of a No. 1 tubular furnace, feeding the raw material medium-temperature asphalt into a No. 1 reaction kettle A from an asphalt inlet on one side of the upper part of the No. 1 reaction kettle A; an asphalt outlet is formed in the other side of the upper part of the No. 1 reaction kettle A, a first middle partition plate is arranged in the middle of the No. 1 reaction kettle A, and an asphalt inlet and an asphalt outlet of the No. 1 reaction kettle A are respectively positioned on two sides of the first middle partition plate; two ends of the first middle partition baffle are fixedly connected with the inner wall of the 1# reaction kettle A respectively, and an asphalt channel is reserved between the bottom of the first middle partition baffle and the bottom of the 1# reaction kettle A; the asphalt entering the space on one side of the No. 1 reaction kettle A from the corresponding asphalt inlet flows downwards, enters the space on the other side of the No. 1 reaction kettle A through the asphalt channel below the first middle partition baffle plate and then flows upwards to the corresponding asphalt outlet;

an asphalt inlet is formed in one side of the upper part of the No. 1 reaction kettle B, a first asphalt full flow pipe is formed in the other side of the interior of the No. 1 reaction kettle B, and a plurality of asphalt full flow ports are formed in the upper part of the first asphalt full flow pipe in the height direction; the asphalt inlet of the No. 1 reaction kettle B is lower than the asphalt outlet of the No. 1 reaction kettle A, and the asphalt inlet and the asphalt outlet are connected through an inclined full-flow pipe I; the asphalt entering the space on one side of the No. 1 reaction kettle B from the corresponding asphalt inlet flows downwards, enters the asphalt full flow pipe I and then flows upwards, and flows out from the corresponding asphalt full flow port; each asphalt full-flow port is respectively connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank through a corresponding asphalt full-flow branch pipe I; a full flow valve I is arranged on the asphalt full flow branch pipe I;

the outlet asphalt of the No. 2 tube furnace enters the No. 2 reaction kettle A from an asphalt inlet at one side of the upper part of the No. 2 reaction kettle A; an asphalt outlet is formed in the other side of the upper part of the No. 2 reaction kettle A, a middle partition plate II is arranged in the middle of the No. 2 reaction kettle A, and an asphalt inlet and an asphalt outlet of the No. 2 reaction kettle A are respectively positioned on two sides of the middle partition plate II; two ends of the middle partition baffle II are fixedly connected with the inner wall of the 2# reaction kettle A respectively, and an asphalt channel is reserved between the bottom of the middle partition baffle II and the bottom of the 2# reaction kettle A; the asphalt entering the space on one side of the No. 2 reaction kettle A from the corresponding asphalt inlet flows downwards, enters the space on the other side of the No. 2 reaction kettle A through the asphalt channel below the middle partition baffle II, and then flows upwards to the corresponding asphalt outlet;

an asphalt inlet is formed in one side of the upper part of the No. 2 reaction kettle B, an asphalt full flow pipe II is formed in the other side of the inside of the No. 2 reaction kettle B, and a plurality of asphalt full flow ports are formed in the upper part of the asphalt full flow pipe II along the height direction; the asphalt inlet of the No. 2 reaction kettle B is lower than the asphalt outlet of the No. 2 reaction kettle A, and the two are connected through a second inclined full flow pipe; the asphalt entering the space on one side of the No. 2 reaction kettle B from the corresponding asphalt inlet flows downwards, enters the asphalt full flow pipe II and then flows upwards, and flows out from the corresponding asphalt full flow port; each asphalt full-flow port is respectively connected with an asphalt inlet at the top of the No. 2 full-flow buffer tank through a corresponding asphalt full-flow branch pipe II; and a full-flow valve II is arranged on the asphalt full-flow branch pipe II.

The circulation amount of the circulating asphalt is 8-10 times of the feeding amount.

The 1# full flow buffer tank is provided with a weight recording control instrument WRC01, the primary modified asphalt pipeline is provided with a first flow regulating valve, and the weight of the 1# full flow buffer tank is maintained to be stable through the first flow regulating valve, so that the asphalt flow sent to the secondary modification reaction is controlled; the 2# full-flow buffer tank is provided with a weight recording control instrument WRC02, the secondary modified asphalt pipeline is provided with a flow regulating valve II, and the weight stability of the 2# full-flow buffer tank is maintained through the flow regulating valve II, so that the asphalt flow sent to the stripping tower is controlled.

The tubular furnace heating method modified asphalt production system with a plurality of serially connected reaction kettles for realizing the process comprises a primary modification reaction unit and a secondary modification reaction unit; the primary modification reaction unit is internally provided with a # 1 tubular furnace, a # 1 reaction kettle A, a # 1 reaction kettle B and a # 1 full flow buffer tank; a No. 2 tubular furnace, a No. 2 reaction kettle A, a No. 2 reaction kettle B and a No. 2 full flow buffer tank are arranged in the secondary modification reaction unit;

the No. 1 tube furnace is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet of the No. 1 tube furnace is connected with the asphalt inlet at the upper part of the No. 1 reaction kettle A through an asphalt outlet pipeline I; the other asphalt outlet pipeline is connected with a medium-temperature asphalt raw material pipeline; the top parts of the No. 1 reaction kettle A and the No. 1 reaction kettle B are respectively provided with a flash evaporation oil gas outlet which is connected with an external stripping tower through a flash evaporation oil gas pipeline; the bottom of the No. 1 reaction kettle A is provided with an asphalt outlet, and the asphalt outlet of the No. 1 reaction kettle A is connected with an asphalt inlet at the upper part of the No. 1 reaction kettle B; an asphalt outlet at the bottom of the No. 1 reaction kettle B is respectively connected with an asphalt full flow pipe I and an asphalt inlet pipeline I, the asphalt inlet pipeline I is additionally connected with an asphalt inlet of the No. 1 tube furnace, and a No. 1 asphalt circulating pump is arranged on the asphalt inlet pipeline I; the asphalt full-flow pipe I is vertically arranged, a plurality of asphalt full-flow ports are formed in the upper portion of the asphalt full-flow pipe I in the height direction, the asphalt full-flow ports are respectively connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank through corresponding asphalt full-flow branch pipes I, and full-flow valves I are respectively arranged on the asphalt full-flow branch pipes I; the No. 1 full flow buffer tank is provided with a weight recording control instrument WRC01, and an asphalt outlet at the bottom of the No. 1 full flow buffer tank is connected with an asphalt inlet pipeline II at the upstream of the No. 2 tube furnace in the secondary upgrading reaction unit through a primary upgraded asphalt pipeline; a first flow regulating valve is arranged on the primary modified asphalt pipeline and is controlled with a weight recording control instrument WRC01 in an interlocking manner;

the 2# tubular furnace is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet of the 2# tubular furnace is connected with the asphalt inlet at the upper part of the 2# reaction kettle A through an asphalt outlet pipeline II; the top parts of the No. 2 reaction kettle A and the No. 2 reaction kettle B are respectively provided with a flash evaporation oil gas outlet which is connected with an external stripping tower through a flash evaporation oil gas pipeline; the bottom of the No. 2 reaction kettle A is provided with an asphalt outlet, and the asphalt outlet of the No. 2 reaction kettle A is connected with an asphalt inlet at the upper part of the No. 2 reaction kettle B; an asphalt outlet at the bottom of the No. 1 reaction kettle B is respectively connected with an asphalt full flow pipe II and an asphalt inlet pipeline II, the asphalt inlet pipeline II is additionally connected with an asphalt inlet of the No. 2 tubular furnace, and a No. 2 asphalt circulating pump is arranged on the asphalt inlet pipeline II; the second asphalt full-flow pipe is vertically arranged, a plurality of asphalt full-flow ports are formed in the upper portion of the second asphalt full-flow pipe in the height direction, the asphalt full-flow ports are respectively connected with asphalt inlets in the top of the No. 2 full-flow buffer tank through corresponding second asphalt full-flow branch pipes, and second full-flow valves are respectively arranged on the second asphalt full-flow branch pipes; the 2# full flow buffer tank is provided with a weight recording control instrument WRC02, and an asphalt outlet at the bottom of the 2# full flow buffer tank is connected with an external stripping tower through a secondary modified asphalt pipeline; and a second flow regulating valve is arranged on the secondary modified asphalt pipeline and is interlocked with the weight recording control instrument WRC02 for control.

the No. 1 tube furnace is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet is connected with the asphalt inlet on one side of the upper part of the No. 1 reaction kettle A through an asphalt outlet pipeline I; the other asphalt outlet pipeline is connected with a medium-temperature asphalt raw material pipeline; the top parts of the No. 1 reaction kettle A and the No. 1 reaction kettle B are respectively provided with a flash evaporation oil gas outlet which is connected with an external stripping tower through a flash evaporation oil gas pipeline; an asphalt outlet is formed in the other side of the upper part of the No. 1 reaction kettle A, and a first middle partition plate is arranged in the No. 1 reaction kettle A between the asphalt inlet and the asphalt outlet; two ends of the first middle partition baffle are fixedly connected with the inner wall of the 1# reaction kettle A respectively, and an asphalt channel is reserved between the bottom of the first middle partition baffle and the bottom of the 1# reaction kettle A; an asphalt inlet is arranged on one side of the upper part of the No. 1 reaction kettle B, and an asphalt full flow pipe I is arranged on the other side in the No. 1 reaction kettle B; the asphalt inlet of the No. 1 reaction kettle B is lower than the asphalt outlet of the No. 1 reaction kettle A, and the asphalt inlet and the asphalt outlet are connected through an inclined full flow pipe I; the bottom of the No. 1 reaction kettle B is provided with an asphalt outlet which is connected with an asphalt inlet of the No. 1 tubular furnace through an asphalt inlet pipeline I, and the asphalt inlet pipeline I is provided with a No. 1 asphalt circulating pump; the upper part of the asphalt full flow pipe I is provided with a plurality of asphalt full flow ports, the asphalt full flow ports are respectively connected with an asphalt inlet at the top of the No. 1 full flow buffer tank through corresponding asphalt full flow branch pipes I, and the asphalt full flow branch pipes I are respectively provided with a full flow valve I; the No. 1 full flow buffer tank is provided with a weight recording control instrument WRC01, and the bottom of the No. 1 asphalt buffer tank is provided with an asphalt outlet which is connected with an asphalt inlet pipeline II at the upstream of the No. 2 tube furnace in the secondary modification reaction unit through a primary modified asphalt pipeline; a first flow regulating valve is arranged on the primary modified asphalt pipeline and is controlled with a weight recording control instrument WRC01 in an interlocking manner;

the No. 2 tube furnace is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet is connected with the asphalt inlet on one side of the upper part of the No. 2 reaction kettle A through an asphalt outlet pipeline II; the top parts of the No. 2 reaction kettle A and the No. 2 reaction kettle B are respectively provided with a flash evaporation oil gas outlet which is connected with an external stripping tower through a flash evaporation oil gas pipeline; an asphalt outlet is formed in the other side of the upper part of the No. 2 reaction kettle A, and a middle partition baffle II is arranged in the No. 2 reaction kettle A between the asphalt inlet and the asphalt outlet; two ends of the middle partition baffle II are fixedly connected with the inner wall of the 2# reaction kettle A respectively, and an asphalt channel is reserved between the bottom of the middle partition baffle II and the bottom of the 2# reaction kettle A; an asphalt inlet is formed in one side of the upper part of the No. 2 reaction kettle B, and an asphalt full flow pipe II is formed in the other side in the No. 2 reaction kettle B; the asphalt inlet of the No. 2 reaction kettle B is lower than the asphalt outlet of the No. 2 reaction kettle A, and the two are connected through a second inclined full-flow pipe; the bottom of the No. 2 reaction kettle B is provided with an asphalt outlet which is connected with an asphalt inlet of the No. 2 tubular furnace through an asphalt inlet pipeline II, and the asphalt inlet pipeline II is provided with a No. 2 asphalt circulating pump; the upper part of the asphalt full flow pipe II is provided with a plurality of asphalt full flow ports, the asphalt full flow ports are respectively connected with an asphalt inlet at the top of the 2# full flow buffer tank through corresponding asphalt full flow branch pipes II, and the asphalt full flow branch pipes II are respectively provided with full flow valves II; the 2# full flow buffer tank is provided with a weight recording control instrument WRC02, and the bottom of the 2# asphalt buffer tank is provided with an asphalt outlet which is connected with an external stripping tower through a secondary modified asphalt pipeline; and a second flow regulating valve is arranged on the secondary modified asphalt pipeline and is interlocked with the weight recording control instrument WRC02 for control.

Compared with the prior art, the invention has the beneficial effects that:

1) in the single modification reaction process (the single-furnace single-kettle stripping flash process comprises a first modification reaction, and the double-furnace double-kettle stripping flash process comprises a first modification reaction and a second modification reaction, namely two modification reactions), a plurality of reaction kettles are adopted for series operation; the prior tar device needs to be matched with two or even a plurality of modified asphalt production lines, and only one modified asphalt production line can meet the requirement at present;

2) compared with the mode of adopting more than two modified asphalt production lines, the mode of adopting the reaction kettles to be connected in series has the advantages that the control system is greatly simplified, the operation and maintenance personnel are reduced, and the production cost is reduced.

3) Compared with the mode of adopting more than two modified asphalt production lines, the mode of adopting the reaction kettles to be connected in series greatly saves the occupied area and the investment cost.

Drawings

FIG. 1 is a first schematic structural diagram of a multi-kettle series tubular furnace heating modified asphalt production system according to the present invention.

FIG. 2 is a schematic structural diagram II of a multi-kettle series tubular furnace heating modified asphalt production system.

In the figure: 1A.1# reaction kettle A1 B.1# reaction kettle B2 A.2# reaction kettle A2 B.2# reaction kettle B3.1 # asphalt circulating pump 4.2# asphalt circulating pump 5.1 # asphalt output pump 6.2 # asphalt output pump 7.1 # tube furnace 8.2 # tube furnace 9.1 # full flow buffer tank 10.2 # full flow buffer tank 11, support lug I12, support lug II 13.1# weighing module 14.2# weighing module 15, middle partition baffle I16, middle partition baffle II 17, asphalt full flow pipe I18, asphalt full flow pipe II 19, full flow valve I20, full flow valve II 21, flow regulating valve I22, flow regulating valve II CWR01, weight recording control instrument I WRC02, weight recording control instrument II

Detailed Description

The following further describes embodiments of the present invention with reference to the accompanying drawings:

as shown in fig. 1 and fig. 2, the production process of modified asphalt by a tubular furnace heating method with multiple serially connected reaction kettles is a single-furnace single-kettle stripping flash evaporation process, and comprises a primary modification reaction process; or the production process of the modified asphalt is a double-furnace double-kettle stripping flash evaporation process, which comprises a primary modification reaction process and a secondary modification reaction process; in the single modification reaction process, more than 2 reaction kettles are adopted for series operation.

The production process of the modified asphalt is a normal-pressure double-furnace double-kettle stripping flash evaporation process, wherein the double kettles are A1 # reaction kettle group and A2 # reaction kettle group, the 1# reaction kettle group is formed by connecting A1 # reaction kettle A1A and A1 # reaction kettle B1B in series, and the 2# reaction kettle group is formed by connecting A2 # reaction kettle A2A and A2 # reaction kettle B2B in series.

As shown in fig. 1 and 2, the production process of the modified asphalt by a multi-reactor series-connected tube furnace heating method specifically comprises the following steps:

1) mixing the raw material medium temperature asphalt with the outlet asphalt of the No. 1 tubular furnace 7, and then sequentially entering a No. 1 reaction kettle A1A and a No. 1 reaction kettle B1B for primary modification reaction; during the primary modification reaction, the temperature in the 1# reaction kettle A1A and the 1# reaction kettle B1B is controlled to be 360-400 ℃, the beta-modification reaction is mainly generated in the asphalt, and flash oil gas generated by flash cracking is discharged to an external stripping tower through a flash oil gas outlet at the top of the corresponding reaction kettle; the asphalt in the No. 1 reaction kettle A1A enters the No. 1 reaction kettle B1B, and the primary modification reaction is completed in the No. 1 reaction kettle B1B;

2) most of the asphalt after the primary upgrading reaction is used as circulating asphalt, the circulating asphalt is sent to a No. 1 tube furnace 7 through a No. 1 asphalt circulating pump 3 to be heated, then the asphalt flows back to a No. 1 reaction kettle A1A and a No. 1 reaction kettle B1B to be used as heat sources, and the residual asphalt flows into a No. 1 full-flow buffer tank 9 through a full-flow valve I19 in a full-flow mode;

3) the asphalt after the primary modification is pumped out from the bottom of a No. 1 full flow buffer tank 9 by a No. 1 asphalt output pump 5 and sequentially enters a No. 2 reaction kettle A2A and a No. 2 reaction kettle B2B through a primary modified asphalt pipeline to carry out secondary modification reaction;

4) mixing the primarily modified asphalt with outlet asphalt of A2 # asphalt circulating pump 4, heating the mixture in A2 # tubular furnace 8, and refluxing the heated mixture to A2 # reaction kettle A2A and A2 # reaction kettle B2B for secondary modification reaction; during the secondary modification reaction, the temperature in A2 # reaction kettle A2A and A2 # reaction kettle B2B is controlled to be 380-420 ℃, and the asphalt simultaneously carries out alpha-modification reaction and beta-modification reaction; the flash oil gas generated by flash cracking is discharged to an external stripping tower through a flash oil gas outlet at the top of the corresponding reaction kettle; the asphalt in the No. 2 reaction kettle A2A enters a No. 2 reaction kettle B2B, and the secondary modification reaction is completed in the No. 2 reaction kettle B2B;

5) most of the asphalt after the secondary modification is used as circulating asphalt, is sent to a No. 2 tubular furnace 8 for heating through a No. 2 asphalt circulating pump 4, and then returns to a No. 2 reaction kettle A2A and a No. 2 reaction kettle B2B to be used as heat sources; the residual asphalt flows into a No. 2 full-flow buffer tank 10 through a second full-flow valve 20 in a full-flow mode;

6) the asphalt after the secondary upgrading is pumped out from the bottom of a 2# full flow buffer tank 10 by a 2# asphalt output pump 6 and sent to a stripping tower through a secondary upgrading asphalt pipeline.

The residence time of the asphalt in the primary modification reaction process is adjusted only by the residence time of the No. 1 reaction kettle B1B, and the residence time of the asphalt in the No. 1 reaction kettle B1B is realized in a full flow mode, namely, the residence time is adjusted by setting different full flow heights; the residence time of the asphalt in the secondary upgrading reaction process is adjusted only by the residence time of the No. 2 reaction kettle B2B, and the residence time of the asphalt in the No. 2 reaction kettle B2B is realized in a full flow mode, namely, the residence time is adjusted by setting different full flow heights.

As shown in fig. 1, after mixing the raw material medium-temperature asphalt with the outlet asphalt of the 1# tubular furnace 7, the raw material medium-temperature asphalt enters the 1# reaction kettle A1A from the asphalt inlet at the upper part of the 1# reaction kettle A1A, flows out from the asphalt outlet at the bottom of the 1# reaction kettle A1A, and then enters the 1# reaction kettle B1B from the asphalt inlet at the upper part of the 1# reaction kettle B1B, and the asphalt outlet arranged at the bottom of the 1# reaction kettle B1B is connected with an asphalt full flow pipe one 17; a plurality of asphalt full-flow ports are formed in the upper edge of the asphalt full-flow pipe I17 in the height direction, each asphalt full-flow port is connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank 9 through a corresponding asphalt full-flow branch pipe I, and a full-flow valve I19 is arranged on each asphalt full-flow branch pipe I;

outlet asphalt of the No. 2 tubular furnace 8 enters the No. 2 reaction kettle A2A from an asphalt inlet at the upper part of the No. 2 reaction kettle A2A, flows out from an asphalt outlet at the bottom of the No. 2 reaction kettle A2A, and then enters the No. 2 reaction kettle B2B from an asphalt inlet at the upper part of the No. 2 reaction kettle B2B, and an asphalt outlet arranged at the bottom of the No. 2 reaction kettle B2B is connected with an asphalt full flow pipe II 18; a plurality of asphalt full-flow ports are arranged on the second asphalt full-flow pipe 18 along the height direction, each asphalt full-flow port is respectively connected with an asphalt inlet at the top of the 2# full-flow buffer tank 10 through a second asphalt full-flow branch pipe, and a second full-flow valve 20 is respectively arranged on the second asphalt full-flow branch pipe.

As shown in fig. 2, the medium temperature asphalt as the raw material was mixed with the asphalt at the outlet of the 1# tube furnace 7 and introduced into the 1# reaction vessel A1A from the asphalt inlet at the upper side of the 1# reaction vessel A1A; the other side of the upper part of the No. 1 reaction kettle A1A is provided with an asphalt outlet, the middle part of the No. 1 reaction kettle A1A is provided with a middle partition baffle plate I15, and an asphalt inlet and an asphalt outlet of the No. 1 reaction kettle A1A are respectively positioned at two sides of the middle partition baffle plate I15; two ends of the middle partition baffle plate I15 are fixedly connected with the inner wall of the No. 1 reaction kettle A1A respectively, and an asphalt channel is reserved between the bottom of the middle partition baffle plate I15 and the bottom of the No. 1 reaction kettle A1A; the asphalt entering the space on one side of the No. 1 reaction kettle A1A from the corresponding asphalt inlet flows downwards, enters the space on the other side of the No. 1 reaction kettle A1A through an asphalt channel below the middle partition plate I15, and then flows upwards to the corresponding asphalt outlet;

an asphalt inlet is arranged on one side of the upper part of the No. 1 reaction kettle B1B, a first asphalt full flow pipe 17 is arranged on the other side in the No. 1 reaction kettle B1B, and a plurality of asphalt full flow ports are arranged on the upper part of the first asphalt full flow pipe 17 along the height direction; the asphalt inlet of the No. 1 reaction kettle B1B is lower than the asphalt outlet of the No. 1 reaction kettle A1A, and the two are connected through a first inclined full-flow pipe; the asphalt entering the space on one side of the No. 1 reaction kettle B1B from the corresponding asphalt inlet flows downwards, enters the asphalt full flow pipe I17, flows upwards and flows out from the corresponding asphalt full flow port; each asphalt full-flow port is respectively connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank 9 through a corresponding asphalt full-flow branch pipe I; a full flow valve I19 is arranged on the asphalt full flow branch pipe I;

the outlet asphalt of the No. 2 tube furnace 8 enters the No. 2 reaction kettle A2A from the asphalt inlet at the upper side of the No. 2 reaction kettle A2A; an asphalt outlet is formed in the other side of the upper portion of the No. 2 reaction kettle A2A, a middle partition baffle II 16 is formed in the middle of the No. 2 reaction kettle A2A, and an asphalt inlet and an asphalt outlet of the No. 2 reaction kettle A2A are respectively located on two sides of the middle partition baffle II 16; two ends of the middle partition baffle II 16 are fixedly connected with the inner wall of the 2# reaction kettle A2A respectively, and an asphalt channel is reserved between the bottom of the middle partition baffle II 16 and the bottom of the 2# reaction kettle A2A; the asphalt entering the space on one side of the No. 2 reaction kettle A2A from the corresponding asphalt inlet flows downwards, enters the space on the other side of the No. 2 reaction kettle A2A through the asphalt channel below the middle partition baffle plate II 16, and then flows upwards to the corresponding asphalt outlet;

an asphalt inlet is arranged on one side of the upper part of the No. 2 reaction kettle B2B, a second asphalt full flow pipe 18 is arranged on the other side in the No. 2 reaction kettle B2B, and a plurality of asphalt full flow ports are arranged on the upper part of the second asphalt full flow pipe 18 along the height direction; the asphalt inlet of the No. 2 reaction kettle B2B is lower than the asphalt outlet of the No. 2 reaction kettle A2A, and the two are connected through an inclined full flow pipe II; the asphalt entering the space on one side of the No. 2 reaction kettle B2B from the corresponding asphalt inlet flows downwards, enters the asphalt full flow pipe II 18 and then flows upwards, and flows out from the corresponding asphalt full flow port; each asphalt full-flow port is respectively connected with an asphalt inlet at the top of the No. 2 full-flow buffer tank 10 through a corresponding asphalt full-flow branch pipe II; and a full flow valve II 20 is arranged on the asphalt full flow branch pipe II.

As shown in fig. 1, the 1# full flow buffer tank 9 is provided with a weight recording control instrument WRC01, the primary modified asphalt pipeline is provided with a flow regulating valve one 21, and the weight of the 1# full flow buffer tank 9 is maintained to be stable through the flow regulating valve one 21, so that the asphalt flow sent to perform the secondary modification reaction is controlled; as shown in fig. 2, the 2# full-flow buffer tank 10 is provided with a weight recording control instrument WRC02, the secondary modified asphalt pipeline is provided with a flow control valve two 22, and the asphalt flow rate to the stripping tower is controlled by maintaining the weight of the 2# full-flow buffer tank 10 stable through the flow control valve two 22.

As shown in fig. 1, the system for producing modified asphalt by a tubular furnace heating method with multiple serially connected reaction kettles for implementing the process comprises a primary modification reaction unit and a secondary modification reaction unit; the primary modification reaction unit is internally provided with A1 # tubular furnace 7, A1 # reaction kettle A1A, A1 # reaction kettle B1B and A1 # full flow buffer tank 9; a2 # tubular furnace 8, A2 # reaction kettle A2A, A2 # reaction kettle B2B and A2 # full flow buffer tank 10 are arranged in the secondary modification reaction unit;

the No. 1 tube furnace 7 is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet of the No. 1 tube furnace 7 is connected with the asphalt inlet at the upper part of the No. 1 reaction kettle A1A through an asphalt outlet pipeline I; the other asphalt outlet pipeline is connected with a medium-temperature asphalt raw material pipeline; the tops of the 1# reaction kettle A1A and the 1# reaction kettle B1B are respectively provided with a flash oil gas outlet which is connected with an external stripping tower through a flash oil gas pipeline; the bottom of the No. 1 reaction kettle A1A is provided with an asphalt outlet, and the asphalt outlet of the No. 1 reaction kettle A1A is connected with an asphalt inlet at the upper part of the No. 1 reaction kettle B1B; an asphalt outlet at the bottom of the No. 1 reaction kettle B1B is respectively connected with an asphalt full flow pipe I17 and an asphalt inlet pipeline I, the asphalt inlet pipeline I is additionally connected with an asphalt inlet of the No. 1 tube furnace 7, and a No. 1 asphalt circulating pump 3 is arranged on the asphalt inlet pipeline I; the asphalt full-flow pipe I17 is vertically arranged, a plurality of asphalt full-flow ports are formed in the upper portion of the asphalt full-flow pipe I along the height direction, the asphalt full-flow ports are respectively connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank 9 through corresponding asphalt full-flow branch pipes I, and full-flow valves I19 are respectively arranged on the asphalt full-flow branch pipes I; the 1# full flow buffer tank 9 is provided with a weight recording control instrument WRC01, and an asphalt outlet at the bottom of the 1# full flow buffer tank 9 is connected with an asphalt inlet pipeline II at the upstream of the 2# tubular furnace 8 in the secondary upgrading reaction unit through a primary upgraded asphalt pipeline; a first flow regulating valve 21 is arranged on the primary modified asphalt pipeline, and the first flow regulating valve 21 and a weight recording control instrument WRC01 are controlled in an interlocking manner;

the 2# tubular furnace 8 is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet of the 2# tubular furnace 8 is connected with the asphalt inlet at the upper part of the 2# reaction kettle A2A through an asphalt outlet pipeline II; the top parts of the No. 2 reaction kettle A2A and the No. 2 reaction kettle B2B are respectively provided with a flash evaporation oil gas outlet which is connected with an external stripping tower through a flash evaporation oil gas pipeline; the bottom of the No. 2 reaction kettle A2A is provided with an asphalt outlet, and the asphalt outlet of the No. 2 reaction kettle A2A is connected with an asphalt inlet at the upper part of the No. 2 reaction kettle B2B; an asphalt outlet at the bottom of the No. 1 reaction kettle B1B is respectively connected with an asphalt full flow pipe II 18 and an asphalt inlet pipeline II, the asphalt inlet pipeline II is additionally connected with an asphalt inlet of the No. 2 tubular furnace 8, and a No. 2 asphalt circulating pump 4 is arranged on the asphalt inlet pipeline II; the second asphalt full-flow pipe 18 is vertically arranged, a plurality of asphalt full-flow ports are formed in the upper portion of the second asphalt full-flow pipe along the height direction, the asphalt full-flow ports are respectively connected with asphalt inlets in the top of the No. 2 full-flow buffer tank 10 through corresponding second asphalt full-flow branch pipes, and the second asphalt full-flow branch pipes are respectively provided with a second full-flow valve 20; the 2# full flow buffer tank 10 is provided with a weight recording control instrument WRC02, and an asphalt outlet at the bottom of the 2# full flow buffer tank 10 is connected with an external stripping tower through a secondary modified asphalt pipeline; and a second flow regulating valve 22 is arranged on the secondary modified asphalt pipeline, and the second flow regulating valve 22 and the weight recording control instrument WRC02 are controlled in an interlocking manner.

As shown in fig. 2, the system for producing modified asphalt by a tubular furnace heating method with multiple serially connected reaction kettles for implementing the process is characterized by comprising a primary modification reaction unit and a secondary modification reaction unit; the primary modification reaction unit is internally provided with A1 # tubular furnace 7, A1 # reaction kettle A1A, A1 # reaction kettle B1B and A1 # full flow buffer tank 9; a2 # tubular furnace 8, A2 # reaction kettle A2A, A2 # reaction kettle B2B and A2 # full flow buffer tank 10 are arranged in the secondary modification reaction unit;

the No. 1 tube furnace 7 is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet is connected with the asphalt inlet on one side of the upper part of the No. 1 reaction kettle A1A through an asphalt outlet pipeline I; the other asphalt outlet pipeline is connected with a medium-temperature asphalt raw material pipeline; the tops of the 1# reaction kettle A1A and the 1# reaction kettle B1B are respectively provided with a flash oil gas outlet which is connected with an external stripping tower through a flash oil gas pipeline; an asphalt outlet is arranged on the other side of the upper part of the No. 1 reaction kettle A1A, and a middle partition baffle plate I15 is arranged in the No. 1 reaction kettle A1A between the asphalt inlet and the asphalt outlet; two ends of the middle partition baffle plate I15 are fixedly connected with the inner wall of the No. 1 reaction kettle A1A respectively, and an asphalt channel is reserved between the bottom of the middle partition baffle plate I15 and the bottom of the No. 1 reaction kettle A1A; an asphalt inlet is arranged on one side of the upper part of the No. 1 reaction kettle B1B, and an asphalt full flow pipe I17 is arranged on the other side in the No. 1 reaction kettle B1B; the asphalt inlet of the No. 1 reaction kettle B1B is lower than the asphalt outlet of the No. 1 reaction kettle A1A, and the two are connected through a first inclined full flow pipe; the bottom of the No. 1 reaction kettle B1B is provided with an asphalt outlet which is connected with an asphalt inlet of the No. 1 tubular furnace 7 through an asphalt inlet pipeline I, and the No. 1 asphalt circulating pump 3 is arranged on the asphalt inlet pipeline I; the upper part of the asphalt full-flow pipe I17 is provided with a plurality of asphalt full-flow ports, the asphalt full-flow ports are respectively connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank 9 through corresponding asphalt full-flow branch pipes I, and the asphalt full-flow branch pipes I are respectively provided with a full-flow valve I19; the No. 1 full flow buffer tank 9 is provided with a weight recording control instrument WRC01, the bottom of the No. 1 asphalt buffer tank 9 is provided with an asphalt outlet which is connected with an asphalt inlet pipeline II at the upstream of the No. 2 tube furnace 8 in the secondary modification reaction unit through a primary modified asphalt pipeline; a first flow regulating valve 21 is arranged on the primary modified asphalt pipeline, and the first flow regulating valve 21 and the weight recording control instrument WRC01 are controlled in an interlocking manner;

the No. 2 tube furnace 8 is provided with an asphalt outlet and an asphalt inlet, and the asphalt outlet is connected with the asphalt inlet on one side of the upper part of the No. 2 reaction kettle A2A through an asphalt outlet pipeline II; the top parts of the No. 2 reaction kettle A2A and the No. 2 reaction kettle B2B are respectively provided with a flash evaporation oil gas outlet which is connected with an external stripping tower through a flash evaporation oil gas pipeline; an asphalt outlet is formed in the other side of the upper part of the No. 2 reaction kettle A2A, and a middle partition baffle plate II 16 is arranged in the No. 2 reaction kettle A2A between the asphalt inlet and the asphalt outlet; two ends of the middle partition baffle II 16 are fixedly connected with the inner wall of the 2# reaction kettle A2A respectively, and an asphalt channel is reserved between the bottom of the middle partition baffle II 16 and the bottom of the 2# reaction kettle A2A; an asphalt inlet is formed in one side of the upper part of the No. 2 reaction kettle B2B, and an asphalt full flow pipe II 18 is formed in the other side in the No. 2 reaction kettle B2B; the asphalt inlet of the No. 2 reaction kettle B2B is lower than the asphalt outlet of the No. 2 reaction kettle A2A, and the two are connected through a second inclined full-flow pipe; the bottom of the No. 2 reaction kettle B2B is provided with an asphalt outlet which is connected with an asphalt inlet of a No. 2 tubular furnace 8 through an asphalt inlet pipeline II, and the asphalt inlet pipeline II is provided with a No. 2 asphalt circulating pump 4; the upper part of the asphalt full-flow pipe II is provided with a plurality of asphalt full-flow ports, the asphalt full-flow ports are respectively connected with an asphalt inlet at the top of the No. 2 full-flow buffer tank 10 through corresponding asphalt full-flow branch pipes II, and the asphalt full-flow branch pipes II are respectively provided with a full-flow valve II 20; the 2# full flow buffer tank 10 is provided with a weight recording control instrument WRC02, and the bottom of the 2# asphalt buffer tank 10 is provided with an asphalt outlet which is connected with an external stripping tower through a secondary modified asphalt pipeline; and a second flow regulating valve 22 is arranged on the secondary modified asphalt pipeline, and the second flow regulating valve 22 and the weight recording control instrument WRC02 are controlled in an interlocking manner.

As shown in fig. 1, in a tubular furnace heating method modified asphalt production system with multiple serially connected reaction kettles, 2 serially connected reaction kettles in a primary modified reaction unit and a secondary modified reaction unit all adopt common empty reaction kettles, and discharge is realized in a full flow mode of an external pipeline; as shown in fig. 2, in the tubular furnace heating modified asphalt production system with multiple serially connected reaction kettles, in the primary modification reaction unit and the secondary modification reaction unit, 2 reaction kettles are serially connected, the reaction kettle a is provided with a middle partition plate inside to prolong the retention time of asphalt, and the reaction kettle B is discharged in a full flow mode through an internal pipeline. In practical engineering design, the technical scheme shown in fig. 1 is easier to realize than the technical scheme shown in fig. 2, and has no problems of heat preservation and emptying, and the length of the pipeline is shorter.

The production process and the system for the modified asphalt by the tubular furnace heating method with the multiple serially connected reaction kettles have the following design ideas:

1. the primary modification reaction process:

1) taking 2 reaction kettles connected in series as an example, namely, the 1# reaction kettle A and the 1# reaction kettle B are connected in series, the raw material medium-temperature asphalt and the circulating asphalt are mixed and then enter the 1# reaction kettle A, and then enter the 1# reaction kettle B in a full flow mode, so that an asphalt intermediate pump can be saved, and the control of the process is simplified.

2) In order to control the residence time of the modified asphalt by the full flow height of the 1# reaction kettle A, safe production can be carried out without liquid level control, the investment of a liquid level meter or a weighing module is saved, and the problem of difficult maintenance is avoided; a middle partition baffle plate I is arranged in a 1# reaction kettle A, the interior of the 1# reaction kettle A is divided into two parts, the two parts are communicated through an asphalt channel below the middle partition baffle plate I, namely, feeding is carried out on one side, full-flow discharging is carried out on the other side, and therefore the latest feeding can be finally discharged; meanwhile, the first middle partition baffle can also play a role in heat exchange to generate a stirring effect, so that the temperature of materials in the whole 1# reaction kettle A is balanced, and the reaction efficiency is improved.

3) In the invention, the circulation amount of the circulating asphalt is set to be 8-10 times of that of the raw material asphalt, so that a certain height difference exists between the 1# reaction kettle A and the 1# reaction kettle B to increase the full-flow speed.

4) The mode that 1# reation kettle B adopted side feeding, the ejection of compact of full flow tube, and the bottom ejection of compact is beaten the circulation and is gone to correspond the tubular furnace heating and then get back to reation kettle as the heat source, need not liquid level control and just can carry out safety in production, has saved the investment of level gauge or weighing module, has avoided the problem of maintenance difficulty, has simplified the control of flow, makes two cauldron pressurization modified pitch production technology of twin-furnace can long-time steady operation.

5) 2 reactors operated in series, only 1# reactor B is provided with a 1# asphalt circulating pump, so that the circulation volume of each reactor can be ensured to be the same and stable, the asphalt discharge volume of each reactor after reaction is ensured to be the same and stable, and the process control is simplified.

6) In order to control the stability and the high pressure of 1# reation kettle B outflow output, 1# full flow buffer tank and 1# pitch output pump have been set up, the discharge capacity of 1# reation kettle B is controlled to the liquid level stability through controlling 1# full flow buffer tank, 1# full flow buffer tank adopts the symmetry to be equipped with the little storage tank of 2 journal stirrup 11 or journal stirrup two 12, adopt 1# weighing module conversion liquid level, owing to only have 2 journal stirrups, can ensure measuring accuracy and stability, and because 1# full flow buffer tank's capacious, it changes and overhauls weighing module easily relatively much.

2. And (3) secondary modification reaction process:

1) taking 2 reaction kettles connected in series as an example, namely, the 1# reaction kettle A and the 1# reaction kettle B are connected in series for operation, and the circulating asphalt enters the 2# reaction kettle A and then enters the 2# reaction kettle B in a full flow mode, so that an asphalt intermediate pump can be saved, and the control of the process is simplified.

2) In order to control the residence time of the modified asphalt by the full flow height of the 2# reaction kettle A, safe production can be carried out without liquid level control, the investment of a liquid level meter or a weighing module is saved, and the problem of difficult maintenance is avoided; a middle partition baffle II is arranged in the 2# reaction kettle A, the interior of the 2# reaction kettle A is divided into two parts, the two parts are communicated through an asphalt channel below the middle partition baffle II, namely, feeding is carried out on one side, full-flow discharging is carried out on the other side, and therefore the latest feeding can be finally discharged; meanwhile, the middle partition baffle II can also play a role in heat exchange to generate a stirring effect, so that the temperature of materials in the whole reaction kettle 1A is balanced, and the reaction efficiency is improved.

3) In the invention, the circulation amount of the circulating asphalt is set to be 8-10 times of that of the raw material asphalt, so that a certain height difference exists between the 2# reaction kettle A and the 2# reaction kettle B to increase the full-flow speed.

4) The mode of side feeding and full flow pipe discharging is adopted in the No. 2 reaction kettle B, the bottom discharging is circulated to heat the corresponding pipe furnace and then returns to the reaction kettle as a heat source, safe production can be carried out without liquid level control, the investment of a liquid level meter or a weighing module is saved, the problem of difficulty in maintenance is avoided, the control of the flow is simplified, and the double-furnace double-kettle pressurizing modified asphalt production process can stably run for a long time.

5) 2 reactors which are operated in series, only 2# reactor B is provided with one 2# asphalt circulating pump, so that the circulation volume of each reactor can be ensured to be the same and stable, the asphalt discharge volume of each reactor after reaction is ensured to be the same and stable, and the control of the process is simplified.

6) In order to control the stability and the high pressure of 2# reation kettle B outflow output, 2# full flow buffer tank and 2# pitch output pump have been set up, the discharge capacity of 2# reation kettle B is controlled to the liquid level stability through controlling 2# full flow buffer tank, 2# full flow buffer tank adopts the symmetry to be equipped with the little storage tank of 2 journal stirrup 11 or journal stirrup two 12, adopt 2# weighing module conversion liquid level, because only there are 2 journal stirrups, can ensure measuring accuracy and stability, and because 2# full flow buffer tank's capacious, it changes and overhauls weighing module easily relatively much.

The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.

Claims

1. The production process of the modified asphalt by a tubular furnace heating method with a plurality of serially connected reaction kettles is a single-furnace single-kettle stripping flash evaporation process and comprises a primary modification reaction process; or the production process of the modified asphalt is a double-furnace double-kettle stripping flash evaporation process, which comprises a primary modification reaction process and a secondary modification reaction process; it is characterized in that more than 2 reaction kettles are adopted for series operation in the single modification reaction process.

2. The process for producing modified asphalt by a tubular furnace heating method through multi-reaction-kettle series connection according to claim 1, wherein the process for producing modified asphalt is an atmospheric pressure double-furnace double-kettle stripping flash distillation process, the double kettles comprise a 1# reaction kettle group and a 2# reaction kettle group, the 1# reaction kettle group comprises a 1# reaction kettle A and a 1# reaction kettle B which are connected in series, and the 2# reaction kettle group comprises a 2# reaction kettle A and a 2# reaction kettle B which are connected in series.

3. The production process of the multi-reactor series-connected tube furnace heating method modified asphalt according to claim 2, which is characterized by comprising the following steps:

4. The process for producing modified asphalt by a tubular furnace heating method with multiple serially connected reaction kettles according to claim 3, wherein the residence time of asphalt in the primary modification reaction process is adjusted by only the residence time of the No. 1 reaction kettle B, and the residence time of asphalt in the No. 1 reaction kettle B is realized by a full flow mode, namely, the residence time is adjusted by setting different full flow heights; the residence time of the asphalt in the secondary upgrading reaction process is adjusted only by the residence time of the 2# reaction kettle B, and the residence time of the asphalt in the 2# reaction kettle B is realized in a full flow mode, namely, the residence time is adjusted by setting different full flow heights.

5. The production process of the modified asphalt by the heating method of the tube furnace with the multiple serially connected reaction kettles according to claim 3, wherein the raw material medium-temperature asphalt is mixed with the asphalt at the outlet of the 1# tube furnace, enters the 1# reaction kettle A from the asphalt inlet at the upper part of the 1# reaction kettle A, flows out from the asphalt outlet at the bottom of the 1# reaction kettle A, enters the 1# reaction kettle B from the asphalt inlet at the upper part of the 1# reaction kettle B, and the asphalt outlet at the bottom of the 1# reaction kettle B is connected with the asphalt full flow tube I; a plurality of asphalt full-flow ports are formed in the upper edge of the asphalt full-flow pipe I in the height direction, each asphalt full-flow port is connected with an asphalt inlet at the top of the No. 1 full-flow buffer tank through a corresponding asphalt full-flow branch pipe I, and a full-flow valve I is arranged on each asphalt full-flow branch pipe I;

6. The production process of the modified asphalt by the heating method of the tube furnace with the multiple serially connected reaction kettles according to claim 3, wherein the raw material medium-temperature asphalt is mixed with the outlet asphalt of the 1# tube furnace and then enters the 1# reaction kettle A from an asphalt inlet at one side of the upper part of the 1# reaction kettle A; an asphalt outlet is formed in the other side of the upper part of the No. 1 reaction kettle A, a first middle partition plate is arranged in the middle of the No. 1 reaction kettle A, and an asphalt inlet and an asphalt outlet of the No. 1 reaction kettle A are respectively positioned on two sides of the first middle partition plate; two ends of the first middle partition baffle are fixedly connected with the inner wall of the 1# reaction kettle A respectively, and an asphalt channel is reserved between the bottom of the first middle partition baffle and the bottom of the 1# reaction kettle A; the asphalt entering the space on one side of the No. 1 reaction kettle A from the corresponding asphalt inlet flows downwards, enters the space on the other side of the No. 1 reaction kettle A through the asphalt channel below the first middle partition baffle plate and then flows upwards to the corresponding asphalt outlet;

7. The production process of the multi-reactor series-connected tube furnace heating method modified asphalt as claimed in claim 3, wherein the circulation amount of the circulating asphalt is 8-10 times of the feeding amount.

8. The process for producing modified asphalt by a tubular furnace heating method with multiple serially connected reaction kettles according to claim 3, wherein a weight recording control instrument WRC01 is arranged on the 1# full-flow buffer tank, a first flow control valve is arranged on the primary modified asphalt pipeline, and the weight of the 1# full-flow buffer tank is maintained to be stable through the first flow control valve, so that the asphalt flow sent to the secondary modification reaction is controlled; the 2# full-flow buffer tank is provided with a weight recording control instrument WRC02, the secondary modified asphalt pipeline is provided with a flow regulating valve II, and the weight stability of the 2# full-flow buffer tank is maintained through the flow regulating valve II, so that the asphalt flow sent to the stripping tower is controlled.

9. The system for producing the modified asphalt by the tubular furnace heating method in the multi-reaction-kettle series connection for realizing the process as claimed in any one of claims 2 to 5 is characterized by comprising a primary modification reaction unit and a secondary modification reaction unit; the primary modification reaction unit is internally provided with a # 1 tubular furnace, a # 1 reaction kettle A, a # 1 reaction kettle B and a # 1 full flow buffer tank; a No. 2 tubular furnace, a No. 2 reaction kettle A, a No. 2 reaction kettle B and a No. 2 full flow buffer tank are arranged in the secondary modification reaction unit;

10. The tubular furnace heating method modified asphalt production system with a plurality of reaction kettles connected in series for realizing the process according to any one of claims 2, 3, 4 and 6 is characterized by comprising a primary modification reaction unit and a secondary modification reaction unit; the primary modification reaction unit is internally provided with a # 1 tubular furnace, a # 1 reaction kettle A, a # 1 reaction kettle B and a # 1 full flow buffer tank; a No. 2 tubular furnace, a No. 2 reaction kettle A, a No. 2 reaction kettle B and a No. 2 full flow buffer tank are arranged in the secondary modification reaction unit;