CN110240917B - System and process for producing modified asphalt by double-furnace double-kettle pressurization - Google Patents
System and process for producing modified asphalt by double-furnace double-kettle pressurization Download PDFInfo
- Publication number
- CN110240917B CN110240917B CN201910656799.2A CN201910656799A CN110240917B CN 110240917 B CN110240917 B CN 110240917B CN 201910656799 A CN201910656799 A CN 201910656799A CN 110240917 B CN110240917 B CN 110240917B
- Authority
- CN
- China
- Prior art keywords
- asphalt
- reaction kettle
- full flow
- reaction
- kettle
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000010426 asphalt Substances 0.000 title claims abstract description 276
- 238000000034 method Methods 0.000 title claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 161
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000007789 gas Substances 0.000 claims abstract description 32
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 23
- 238000006011 modification reaction Methods 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 21
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000012986 modification Methods 0.000 claims description 5
- 230000004048 modification Effects 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
- 238000005086 pumping Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 abstract description 39
- 238000005303 weighing Methods 0.000 abstract description 10
- 238000007599 discharging Methods 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 238000012423 maintenance Methods 0.000 abstract description 6
- 238000005259 measurement Methods 0.000 description 14
- 230000008020 evaporation Effects 0.000 description 10
- 238000001704 evaporation Methods 0.000 description 10
- 238000007667 floating Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000691 measurement method Methods 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 238000003908 quality control method Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000011883 electrode binding agent Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000010667 large scale reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000007039 two-step reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C3/00—Working-up pitch, asphalt, bitumen
- C10C3/02—Working-up pitch, asphalt, bitumen by chemical means reaction
Landscapes
- Chemical & Material Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Civil Engineering (AREA)
- Structural Engineering (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Working-Up Tar And Pitch (AREA)
Abstract
The invention relates to a system and a process for producing modified asphalt by double-furnace double-kettle pressurization, wherein the system comprises a 1# reaction kettle, a 1# tubular furnace, a 2# reaction kettle and a 2# tubular furnace; the top of the No. 1 reaction kettle is provided with a nitrogen inlet I and a flash oil gas outlet I, one side of the upper part is provided with an asphalt feed inlet I, the other side of the upper part is provided with an asphalt full flow port I, the bottom of the reaction kettle is provided with a circulating asphalt outlet I, the inside of the reaction kettle is provided with a flexible baffle I, the top of the No. 2 reaction kettle is provided with a nitrogen inlet II and a flash oil gas outlet II, one side of the upper part is provided with an asphalt feed inlet II, the other side of the upper part is provided with an asphalt full flow port II, and the bottom of the reaction kettle is provided with a circulating asphalt outlet II; and a second flexible baffle is arranged in the inner part. According to the invention, the reaction kettle is changed from a side feeding mode to a lower discharging mode to a side feeding mode and a full discharging mode, the lower discharging is circulated, the safe production is realized without liquid level control, the investment of a liquid level meter or a weighing module is saved, the difficult problem of difficult maintenance of the liquid level meter or the weighing module is solved, the control method of the flow is simplified, and the system can stably operate for a long time.
Description
Technical Field
The invention relates to the technical field of metallurgical coking, in particular to a system and a process for producing modified asphalt by double-furnace double-kettle pressurization.
Background
Asphalt is generally produced by about 50% -60% in the coal tar processing process, and the larger the processing scale, the more asphalt yield is, which belongs to a large amount of products for tar processing. The modified asphalt is a main downstream product of the current asphalt, and is mainly used for producing prebaked anodes and preparing battery bars or electrode binders in the electrolytic aluminum industry.
At present, the technology for producing modified asphalt in China mostly adopts a thermal polycondensation method, and the thermal polycondensation method can be divided into a kettle type heating method and a tubular furnace heating method according to a heating mode.
The kettle type heating process for producing modified asphalt uses medium temperature asphalt as material and includes heating the outer surface of the reaction kettle with heating furnace to control certain reaction residence time and proper reaction temperature. Because the heating surface is the outer surface of the reaction kettle, in order to achieve good mass and heat transfer effect, a stirrer is required to be arranged in the reaction kettle, so that the volume of the reaction kettle is limited, and the design capacity is limited.
The modified asphalt production process by a tube furnace heating method comprises a pressurized double-furnace double-kettle stripping flash evaporation process introduced from France, a domestic normal-pressure or reduced-pressure double-furnace double-kettle stripping flash evaporation process, a single-furnace single-kettle stripping flash evaporation process and the like; the double-kettle double-furnace stripping flash evaporation process takes medium-temperature asphalt as a raw material, asphalt heating is carried out in a tubular heating furnace, and then modification reaction is carried out in a reaction kettle; the reaction is carried out in two steps, and can be normal pressure, pressurized or depressurized according to different product requirements, and the modified asphalt product is obtained by flash evaporation and steam stripping through a steam stripping tower after the reaction. The process has the advantages that the two-step reaction is adopted, the generation amount of the alpha-component and the beta-component can be effectively controlled, the product quality is controllable, and the stripping method is adopted to separate asphalt and oil products, thereby being beneficial to the adjustment of softening points. The single-furnace single-kettle stripping flash evaporation process also uses medium-temperature asphalt as a raw material, asphalt is heated in a tubular heating furnace, then the reaction is carried out in a reaction kettle, the reaction is completed in one step, flash evaporation and stripping are carried out in a stripping tower after the reaction, and only the product quality control is not flexible by the double-furnace double-kettle stripping flash evaporation process.
The modified asphalt production process by the tube furnace heating method has great design capability and flexible reaction control, and becomes the main stream of the current modified asphalt production process, but has a great problem that the liquid level measurement of a modified asphalt reaction kettle is difficult to solve, because the modified asphalt reaction kettle achieves the aim of asphalt modification by controlling the residence time and the reaction temperature of reactants, and the residence time is controlled by controlling the liquid level of the reaction kettle, the liquid level measurement is the key of reaction process control.
The traditional reaction kettle liquid level remote-transmission measurement method generally adopts a pressure difference measurement mode, and is converted into liquid level height through density calculation of liquid, but due to the particularities of asphalt liquid, the temperature in the reaction kettle is higher than 380 ℃, solid suspended matters such as polymer and the like are contained in the liquid, the viscosity of the liquid is high, solidification is easy, the evaporation amount of asphalt smoke is high, condensation is easy, and the like, asphalt is easy to solidify and block at a pressure measuring interface of instrument liquid, so that a measuring instrument is malfunctioning. If the float level gauge is adopted, the float and the guide cylinder or the guide steel wire are easy to adhere together and are not easy to float up and down, so that the liquid level measurement cannot be realized. In addition, there are also attempts to use a floating ball level gauge, but because the liquid level of the reaction kettle is up to more than 10m, the traditional floating ball level gauge has a liquid level indicator with the same height as the liquid level, so that the lifting rod of the floating ball level gauge is too long, the liquid level indicator is too high at the top of the kettle and is difficult to realize, and the floating ball and the guide cylinder or the guide steel wire are easy to adhere together and are difficult to float up and down. In addition, asphalt fume easily enters the liquid level indicator along the lifting rod of the liquid level indicator to generate condensation, so that the liquid level indicator is blocked. If the radar liquid level gauge is adopted, the short-time measurement effect is still possible, but because asphalt smoke is easy to condense on the radar liquid level gauge, the radar electromagnetic wave receiving is quickly disabled, and the maintenance is frequent.
In the pressurized double-furnace double-kettle stripping flash evaporation technology introduced in France, the liquid level of the reaction kettle is controlled by converting the liquid level by a weighing module instead of a liquid level measurement method, the liquid level is controlled by controlling the whole weight of the reaction kettle, the measurement points of the weighing module are the key for measuring the accuracy of weight, generally 2 measurement points are more accurate, the lugs of the large-scale reaction kettle are usually 6 or 8, the measurement is inaccurate, and are often influenced by wind load and weighing module errors, so that the weight measurement is unstable and the fluctuation is large, the converted liquid level is unstable, the fluctuation of the outflow quantity of modified asphalt is large, and the quality control of the modified asphalt is influenced. Meanwhile, because the appearance of the reaction kettle equipment is huge, the maintenance and replacement of the weighing module are very difficult, the maintenance time is long, and the normal production is seriously influenced.
In summary, in the current modified asphalt production process by the tubular furnace heating method, the problem of liquid level measurement of the reaction kettle is not well solved, so that the automation control of the process needs to be perfected, and the process and equipment need to be improved.
Disclosure of Invention
The invention provides a system and a process for producing modified asphalt by pressurizing double furnaces and double kettles, wherein a reaction kettle is changed into side feeding and full-flow discharging from side feeding and lower discharging modes, the lower discharging is circularly discharged to be heated by a tubular furnace and returned to the reaction kettle as a heat source, the safe production can be realized without liquid level control, the investment of a liquid level meter or a weighing module is saved, the difficult problem of difficult maintenance of the liquid level meter or the weighing module is solved, the control method of the flow is simplified, and the system can stably operate for a long time.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
A system for producing modified asphalt by double-furnace double-kettle pressurization comprises a 1# reaction kettle, a 1# tubular furnace, a 2# reaction kettle and a 2# tubular furnace; the top of the No. 1 reaction kettle is provided with a nitrogen inlet I and a flash oil gas outlet I, one side of the upper part is provided with an asphalt feed inlet I, the other side of the upper part is provided with an asphalt full flow port I, and the bottom is provided with a circulating asphalt outlet I; a flexible baffle I with a snakelike cross section is arranged in the 1# reaction kettle close to one side of an asphalt full flow port I, the flexible baffle I divides the 1# reaction kettle into a main reaction area and a full flow area, an asphalt feed port I is positioned at one side of the main reaction area, the asphalt full flow port I is positioned at one side of the full flow area, and the main reaction area is communicated with the full flow area through an asphalt flow channel I below the flexible baffle; the first asphalt circulating loop is sequentially provided with a No. 1 asphalt circulating pump, a No. 1 tubular furnace and a raw asphalt inlet along the asphalt conveying direction, and the raw asphalt inlet is connected with an external raw asphalt conveying pipeline; the top of the No. 2 reaction kettle is provided with a nitrogen inlet II and a flash oil gas outlet II, one side of the upper part is provided with an asphalt feed inlet II, the other side of the upper part is provided with an asphalt full flow port II, and the bottom of the reaction kettle is provided with a circulating asphalt outlet II; a flexible baffle II with a snakelike cross section is arranged in the 2# reaction kettle close to one side of the asphalt full flow port II, the flexible baffle II divides the 2# reaction kettle into a main reaction area and a full flow area, the asphalt feed port II is positioned at one side of the main reaction area, the asphalt full flow port II is positioned at one side of the full flow area, and the main reaction area is communicated with the full flow area through an asphalt flow channel II below the flexible baffle II; the second asphalt circulating loop is connected with the second asphalt feeding port through a second asphalt circulating loop, and a No. 2 asphalt circulating pump, an injection mixer and a No. 2 tubular furnace are sequentially arranged on the second asphalt circulating loop along the asphalt conveying direction; the asphalt full flow port I of the No. 1 reaction kettle is connected with a jet mixer through a primary modified asphalt conveying pipeline; the asphalt full flow port II of the No. 2 reaction kettle is connected with the modified asphalt inlet of the normal pressure stripping tower through a secondary modified asphalt conveying pipeline; the first nitrogen inlet of the No. 1 reaction kettle and the second nitrogen inlet of the No. 2 reaction kettle are respectively connected with an external nitrogen conveying pipeline, and the first flash oil gas outlet of the No. 1 reaction kettle and the second flash oil gas outlet of the No. 2 reaction kettle are connected with the oil gas inlet of the normal pressure stripping tower through the flash oil gas conveying pipelines.
The No. 1 reaction kettle is provided with a plurality of asphalt full flow ports I along the height direction, each asphalt full flow port I is connected with a primary modified asphalt conveying pipeline through an asphalt full flow pipe I, and full flow valves I are respectively arranged on the asphalt full flow pipes I; and a plurality of asphalt full flow ports II are arranged along the upper edge of the No.2 reaction kettle in the height direction, each asphalt full flow port II is connected with a secondary modified asphalt conveying pipeline through an asphalt full flow pipe II, and full flow valves II are respectively arranged on the asphalt full flow pipes II.
The top surface of the first flexible baffle is higher than the top surface of the first asphalt full flow port of Yu Zuishang square; the top surface of the second flexible baffle plate is higher than the top surface of the Yu Zuishang square asphalt full flow port.
The bottom of the No.1 reaction kettle is cone-shaped, and a circulating asphalt outlet I is arranged in the center of the cone-shaped bottom; the bottom of the 2# reaction kettle is cone-shaped, and the second circulating asphalt outlet is arranged in the center of the cone-shaped bottom.
A process for producing modified asphalt by double-furnace double-kettle pressurization comprises the following steps:
1) Mixing the medium-temperature asphalt and asphalt at the outlet of the 1# tubular furnace, then entering a 1# reaction kettle from an asphalt feed inlet I, and introducing nitrogen into the 1# reaction kettle, wherein the temperature is controlled to be 360-400 ℃, and the pressure is controlled to be 250-350 kPa; the mixed asphalt entering the No.1 reaction kettle flows from top to bottom in a main reaction zone, bypasses a flexible baffle plate through an asphalt flow channel at the bottom and flows from bottom to top in a full flow zone, and in the process, the mixed asphalt undergoes primary modification reaction mainly comprising beta-modification reaction; the primary modified asphalt flows out through an asphalt full flow port I; flash oil gas generated by the primary modification reaction is discharged into the normal pressure stripping tower through a flash oil gas outlet at the top of the No.1 reaction kettle;
2) The asphalt at the bottom of the No. 1 reaction kettle is pumped out by a No. 1 asphalt circulating pump, the flow rate of the asphalt during pumping out is 7-9 times that of the full-flow discharged asphalt, the pumped asphalt is sent to a No. 1 tubular furnace for heating, and then the asphalt is circulated back to the asphalt feeding port of the No. 1 reaction kettle for heating the medium-temperature asphalt of the raw material;
3) The primary modified asphalt flowing out of the full asphalt port I of the No. 1 reaction kettle automatically flows into an injection mixer, is mixed with the secondary modified asphalt pumped out of the bottom of the No. 2 reaction kettle in the injection mixer, is sucked into a second asphalt circulation loop through vacuum generated by the injection mixer, is heated by a No. 2 tubular furnace, and then enters the No. 2 reaction kettle from an asphalt feed port II; nitrogen is introduced into the 2# reaction kettle, the temperature is controlled at 380-420 ℃, and the pressure is controlled at 250-350 kPa; the mixed asphalt entering the 2# reaction kettle flows from top to bottom in a main reaction zone, bypasses a second flexible baffle through an asphalt flow channel at the bottom and flows from bottom to top in a full flow zone, and in the process, the mixed asphalt is subjected to secondary modification reaction which is carried out simultaneously by alpha-modification reaction and beta-modification reaction; flash oil gas generated by the secondary modification reaction is discharged to the normal pressure stripping tower through a flash oil gas outlet II at the top of the No. 2 reaction kettle; and (3) the asphalt subjected to secondary modification flows out from the asphalt full-flow port II, and is subjected to back pressure self-flow to the normal pressure stripping tower for stripping, so that a modified asphalt finished product is obtained.
Compared with the prior art, the invention has the beneficial effects that:
1) The existing modified asphalt reaction kettle of the double-furnace double-kettle pressurizing modified asphalt production process adopts a mode of side feeding and bottom discharging, one part of discharged materials is heated back to the reaction kettle through a tube furnace to serve as a heat source, the liquid level or weight of the reaction kettle is kept constant by controlling the flow of the other part of discharged materials, and then the reaction residence time of the modified asphalt is controlled; the liquid level measurement is difficult and the weight measurement is unstable, so that the operation of the whole process is unstable, and the product quality is influenced; according to the invention, the modified asphalt reaction kettle adopts a mode of side feeding, bottom discharging, heating, circulating and full-flow discharging, a plurality of full-flow ports are arranged according to the preset residence time, and the reaction residence time of the modified asphalt is controlled through the full-flow height, so that the influence caused by difficult liquid level measurement and unstable weight measurement can be avoided, and the operation of the modified asphalt reaction kettle can be smoothly and smoothly operated without liquid level display;
2) A flexible baffle plate is arranged near one side of the full flow port of the asphalt in the modification reaction kettle (the volume of the main reaction zone is larger than that of the full flow zone because the flow rate of the asphalt for heating by circulating is about 8 times that of the asphalt discharged by full flow, and the asphalt is ensured to be fed in and out after first in and first out in the modification reaction kettle;
3) The flexible baffle plate not only plays a role in separating areas, but also plays a role in heat exchange, and can produce a stirring effect, so that the temperature of materials in the whole reaction kettle is balanced, and the reaction efficiency is improved;
4) The system can realize safe production without liquid level control, so that the investment of a liquid level meter or a weighing module is saved, the difficult problem of difficult maintenance of the liquid level meter or the weighing module is solved, and the control method of the flow is simplified.
Drawings
FIG. 1 is a schematic diagram of a system for producing modified asphalt by pressurizing with two furnaces and two kettles.
FIG. 2 is a view A-A/B-B of FIG. 1.
In the figure: 1.1# reactor 2. Flexible baffle-3.1 # asphalt circulating pump 4.1# tube furnace 5. Full flow valve-6.2 # reactor 7. Flexible baffle-8.2 # asphalt circulating pump 9.2 # tube furnace 10. Full flow valve-11. Jet mixer
Detailed Description
The following is a further description of embodiments of the invention, taken in conjunction with the accompanying drawings:
As shown in FIG. 1, the system for producing modified asphalt by double-furnace double-kettle pressurization comprises a 1# reaction kettle 1, a 1# tubular furnace 4, a 2# reaction kettle 6 and a 2# tubular furnace 9; the top of the 1# reaction kettle 1 is provided with a nitrogen inlet I and a flash oil gas outlet I, one side of the upper part is provided with an asphalt feed inlet I, the other side of the upper part is provided with an asphalt full flow port I, and the bottom is provided with a circulating asphalt outlet I; a flexible baffle I2 (shown in figure 2) with a snakelike cross section is arranged in the 1# reaction kettle 1 near one side of an asphalt full flow port, the flexible baffle I2 divides the 1# reaction kettle 1 into a main reaction area and a full flow area, an asphalt feeding port I is positioned at one side of the main reaction area, an asphalt full flow port I is positioned at one side of the full flow area, and the main reaction area is communicated with the full flow area through an asphalt flow channel I below the flexible baffle I2; the first asphalt circulating loop is sequentially provided with a No. 1 asphalt circulating pump 3, a No. 1 tubular furnace 4 and a raw asphalt inlet along the asphalt conveying direction, and the raw asphalt inlet is connected with an external raw asphalt conveying pipeline; the top of the No. 2 reaction kettle 6 is provided with a nitrogen inlet II and a flash oil gas outlet II, one side of the upper part is provided with an asphalt feed inlet II, the other side of the upper part is provided with an asphalt full flow port II, and the bottom is provided with a circulating asphalt outlet II; a flexible baffle plate II 7 (shown in figure 2) with a serpentine cross section is arranged in the 2# reaction kettle 6 near the asphalt full flow port II, the flexible baffle plate II divides the 2# reaction kettle 6 into a main reaction area and a full flow area, the asphalt feed port II is positioned at one side of the main reaction area, the asphalt full flow port II is positioned at one side of the full flow area, and the main reaction area is communicated with the full flow area through an asphalt flow channel II below the flexible baffle plate II 7; the second asphalt recycling outlet is connected with the second asphalt feeding port through a second asphalt recycling loop, and a No. 2 asphalt recycling pump 8, an injection mixer 11 and a No. 2 tubular furnace 9 are sequentially arranged on the second asphalt recycling loop along the asphalt conveying direction; the first asphalt full flow port of the 1# reaction kettle 1 is connected with a jet mixer 11 through a primary modified asphalt conveying pipeline; the asphalt full flow port II of the No. 2 reaction kettle 6 is connected with the modified asphalt inlet of the normal pressure stripping tower through a secondary modified asphalt conveying pipeline; the nitrogen inlet I of the 1# reaction kettle 1 and the nitrogen inlet II of the 2# reaction kettle 6 are respectively connected with an external nitrogen conveying pipeline, and the flash oil gas outlet I of the 1# reaction kettle 1 and the flash oil gas outlet II of the 2# reaction kettle 6 are connected with the oil gas inlet of the normal pressure stripping tower through the flash oil gas conveying pipelines.
The 1# reaction kettle 1 is provided with a plurality of asphalt full flow ports I along the height direction, each asphalt full flow port I is connected with a primary modified asphalt conveying pipeline through an asphalt full flow pipe I, and the asphalt full flow pipes I are respectively provided with full flow valves I5; and a plurality of asphalt full flow ports II are arranged on the upper edge of the No.2 reaction kettle 6 in the high direction, each asphalt full flow port II is connected with a secondary modified asphalt conveying pipeline through an asphalt full flow pipe II, and full flow valves II 10 are respectively arranged on the asphalt full flow pipes II.
The top surface of the first flexible baffle plate 2 is higher than the full-flow opening I of Yu Zuishang square asphalt; the top surface of the second flexible baffle 7 is higher than the top surface of the second asphalt full flow port Yu Zuishang.
The bottom of the 1# reaction kettle 1 is cone-shaped, and a circulating asphalt outlet I is arranged in the center of the cone-shaped bottom; the bottom of the 2# reaction kettle 6 is cone-shaped, and the second circulating asphalt outlet is arranged in the center of the cone-shaped bottom.
The invention relates to a process for producing modified asphalt by double-furnace double-kettle pressurization, which comprises the following steps:
1) Mixing the medium-temperature asphalt and asphalt at the outlet of the 1# tubular furnace, then introducing nitrogen into the 1# reaction kettle 1 from the first asphalt feed inlet, wherein the temperature is controlled at 360-400 ℃, and the pressure is controlled at 250-350 kPa; the mixed asphalt entering the 1# reaction kettle 1 flows from top to bottom in a main reaction zone, bypasses a flexible baffle I2 through an asphalt flow channel at the bottom and then flows from bottom to top in a full flow zone, and in the process, the mixed asphalt undergoes primary modification reaction mainly comprising beta-modification reaction; the primary modified asphalt flows out through an asphalt full flow port I; flash oil gas generated by the primary modification reaction is discharged into an atmospheric stripping tower through a flash oil gas outlet at the top of a 1# reaction kettle 1;
2) The asphalt at the bottom of the 1# reaction kettle 1 is pumped out by a 1# asphalt circulating pump 3, the flow rate of the asphalt during pumping out is 7-9 times that of the full-flow discharged asphalt, the pumped asphalt is sent to a 1# tubular furnace 4 for heating, and then the asphalt is circulated back to the asphalt feeding port of the 1# reaction kettle 1 for heating the medium-temperature asphalt of the raw material;
3) The primary modified asphalt flowing out of the full asphalt port I of the No. 1 reaction kettle 1 automatically flows into the jet mixer 11, is mixed with the secondary modified asphalt pumped out of the bottom of the No. 2 reaction kettle 6 in the jet mixer 11, is sucked into a second asphalt circulation loop through vacuum generated by the jet mixer 11, is heated by the No. 2 tubular furnace 9, and then enters the No. 2 reaction kettle 6 from the asphalt feed port II; nitrogen is introduced into the 2# reaction kettle 6, the temperature is controlled at 380-420 ℃, and the pressure is controlled at 250-350 kPa; the mixed asphalt entering the 2# reaction kettle 6 flows from top to bottom in a main reaction zone, bypasses the flexible baffle II 7 through an asphalt flow channel at the bottom and then flows from bottom to top in a full flow zone, and in the process, the mixed asphalt is subjected to secondary modification reaction which is carried out simultaneously by alpha-modification reaction and beta-modification reaction; flash oil gas generated by the secondary modification reaction is discharged to the normal pressure stripping tower through a flash oil gas outlet on the top of the 2# reaction kettle 6; and (3) the asphalt subjected to secondary modification flows out from the asphalt full-flow port II, and is subjected to back pressure self-flow to the normal pressure stripping tower for stripping, so that a modified asphalt finished product is obtained.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (5)
1. A system for producing modified asphalt by double-furnace double-kettle pressurization is characterized by comprising a 1# reaction kettle, a 1# tubular furnace, a 2# reaction kettle and a 2# tubular furnace; the top of the No. 1 reaction kettle is provided with a nitrogen inlet I and a flash oil gas outlet I, one side of the upper part is provided with an asphalt feed inlet I, the other side of the upper part is provided with an asphalt full flow port I, and the bottom is provided with a circulating asphalt outlet I; a flexible baffle I with a snakelike cross section is arranged in the 1# reaction kettle close to one side of an asphalt full flow port I, the flexible baffle I divides the 1# reaction kettle into a main reaction area and a full flow area, an asphalt feed port I is positioned at one side of the main reaction area, the asphalt full flow port I is positioned at one side of the full flow area, and the main reaction area is communicated with the full flow area through an asphalt flow channel I below the flexible baffle; the first asphalt circulating loop is sequentially provided with a No. 1 asphalt circulating pump, a No. 1 tubular furnace and a raw asphalt inlet along the asphalt conveying direction, and the raw asphalt inlet is connected with an external raw asphalt conveying pipeline; the top of the No. 2 reaction kettle is provided with a nitrogen inlet II and a flash oil gas outlet II, one side of the upper part is provided with an asphalt feed inlet II, the other side of the upper part is provided with an asphalt full flow port II, and the bottom of the reaction kettle is provided with a circulating asphalt outlet II; a flexible baffle II with a snakelike cross section is arranged in the 2# reaction kettle close to one side of the asphalt full flow port II, the flexible baffle II divides the 2# reaction kettle into a main reaction area and a full flow area, the asphalt feed port II is positioned at one side of the main reaction area, the asphalt full flow port II is positioned at one side of the full flow area, and the main reaction area is communicated with the full flow area through an asphalt flow channel II below the flexible baffle II; the second asphalt circulating loop is connected with the second asphalt feeding port through a second asphalt circulating loop, and a No. 2 asphalt circulating pump, an injection mixer and a No. 2 tubular furnace are sequentially arranged on the second asphalt circulating loop along the asphalt conveying direction; the asphalt full flow port I of the No. 1 reaction kettle is connected with a jet mixer through a primary modified asphalt conveying pipeline; the asphalt full flow port II of the No. 2 reaction kettle is connected with the modified asphalt inlet of the normal pressure stripping tower through a secondary modified asphalt conveying pipeline; the first nitrogen inlet of the No. 1 reaction kettle and the second nitrogen inlet of the No. 2 reaction kettle are respectively connected with an external nitrogen conveying pipeline, and the first flash oil gas outlet of the No. 1 reaction kettle and the second flash oil gas outlet of the No. 2 reaction kettle are connected with the oil gas inlet of the normal pressure stripping tower through the flash oil gas conveying pipelines.
2. The system for producing modified asphalt by pressurizing two furnaces and two kettles according to claim 1, wherein the No. 1 reaction kettle is provided with a plurality of asphalt full flow ports I along the height direction, each asphalt full flow port I is respectively connected with a primary modified asphalt conveying pipeline through an asphalt full flow pipe I, and the asphalt full flow pipes I are respectively provided with full flow valves I; and a plurality of asphalt full flow ports II are arranged along the upper edge of the No. 2 reaction kettle in the height direction, each asphalt full flow port II is connected with a secondary modified asphalt conveying pipeline through an asphalt full flow pipe II, and full flow valves II are respectively arranged on the asphalt full flow pipes II.
3. The system for producing modified asphalt by double-furnace double-kettle pressurization according to claim 1, wherein the top surface of the first flexible baffle is higher than the full flow port of Yu Zuishang square asphalt; the top surface of the second flexible baffle plate is higher than the top surface of the Yu Zuishang square asphalt full flow port.
4. The system for producing modified asphalt by double-furnace double-kettle pressurization according to claim 1, wherein the bottom of the No. 1 reaction kettle is cone-shaped, and the circulating asphalt outlet is arranged in the center of the cone-shaped bottom; the bottom of the 2# reaction kettle is cone-shaped, and the second circulating asphalt outlet is arranged in the center of the cone-shaped bottom.
5. A process for producing modified asphalt by double-furnace double-kettle pressurization is characterized by comprising the following steps:
1) Mixing the medium-temperature asphalt and asphalt at the outlet of the 1# tubular furnace, then entering a 1# reaction kettle from an asphalt feed inlet I, and introducing nitrogen into the 1# reaction kettle, wherein the temperature is controlled to be 360-400 ℃, and the pressure is controlled to be 250-350 kPa; the mixed asphalt entering the No.1 reaction kettle flows from top to bottom in a main reaction zone, bypasses a flexible baffle plate through an asphalt flow channel at the bottom and flows from bottom to top in a full flow zone, and in the process, the mixed asphalt undergoes primary modification reaction mainly comprising beta-modification reaction; the primary modified asphalt flows out through an asphalt full flow port I; flash oil gas generated by the primary modification reaction is discharged into the normal pressure stripping tower through a flash oil gas outlet at the top of the No.1 reaction kettle;
2) The asphalt at the bottom of the No. 1 reaction kettle is pumped out by a No. 1 asphalt circulating pump, the flow rate of the asphalt during pumping out is 7-9 times that of the full-flow discharged asphalt, the pumped asphalt is sent to a No. 1 tubular furnace for heating, and then the asphalt is circulated back to the asphalt feeding port of the No. 1 reaction kettle for heating the medium-temperature asphalt of the raw material;
3) The primary modified asphalt flowing out of the full asphalt port I of the No. 1 reaction kettle automatically flows into an injection mixer, is mixed with the secondary modified asphalt pumped out of the bottom of the No. 2 reaction kettle in the injection mixer, is sucked into a second asphalt circulation loop through vacuum generated by the injection mixer, is heated by a No. 2 tubular furnace, and then enters the No. 2 reaction kettle from an asphalt feed port II; nitrogen is introduced into the 2# reaction kettle, the temperature is controlled at 380-420 ℃, and the pressure is controlled at 250-350 kPa; the mixed asphalt entering the 2# reaction kettle flows from top to bottom in a main reaction zone, bypasses a second flexible baffle through an asphalt flow channel at the bottom and flows from bottom to top in a full flow zone, and in the process, the mixed asphalt is subjected to secondary modification reaction which is carried out simultaneously by alpha-modification reaction and beta-modification reaction; flash oil gas generated by the secondary modification reaction is discharged to the normal pressure stripping tower through a flash oil gas outlet II at the top of the No. 2 reaction kettle; and (3) the asphalt subjected to secondary modification flows out from the asphalt full-flow port II, and is subjected to back pressure self-flow to the normal pressure stripping tower for stripping, so that a modified asphalt finished product is obtained.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910656799.2A CN110240917B (en) | 2019-07-19 | 2019-07-19 | System and process for producing modified asphalt by double-furnace double-kettle pressurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910656799.2A CN110240917B (en) | 2019-07-19 | 2019-07-19 | System and process for producing modified asphalt by double-furnace double-kettle pressurization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110240917A CN110240917A (en) | 2019-09-17 |
| CN110240917B true CN110240917B (en) | 2024-04-26 |
Family
ID=67893147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910656799.2A Active CN110240917B (en) | 2019-07-19 | 2019-07-19 | System and process for producing modified asphalt by double-furnace double-kettle pressurization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110240917B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111203169A (en) * | 2020-03-06 | 2020-05-29 | 中冶焦耐(大连)工程技术有限公司 | Modified asphalt reaction kettle with side feeding and full flow discharging functions |
| CN112745870A (en) * | 2020-12-24 | 2021-05-04 | 中冶焦耐(大连)工程技术有限公司 | Modified asphalt production system and process adopting horizontal reaction kettle |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057740A (en) * | 2017-06-20 | 2017-08-18 | 中冶焦耐(大连)工程技术有限公司 | A kind of Existing in Improved Pitch Production System |
| CN107245346A (en) * | 2017-06-20 | 2017-10-13 | 中冶焦耐(大连)工程技术有限公司 | A kind of Production Process for Modified Pitch |
| CN206887030U (en) * | 2017-06-20 | 2018-01-16 | 中冶焦耐(大连)工程技术有限公司 | A kind of Existing in Improved Pitch Production System |
| CN210340778U (en) * | 2019-07-19 | 2020-04-17 | 中冶焦耐(大连)工程技术有限公司 | System for two cauldron pressurization production modified pitch of twin-furnace |
-
2019
- 2019-07-19 CN CN201910656799.2A patent/CN110240917B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057740A (en) * | 2017-06-20 | 2017-08-18 | 中冶焦耐(大连)工程技术有限公司 | A kind of Existing in Improved Pitch Production System |
| CN107245346A (en) * | 2017-06-20 | 2017-10-13 | 中冶焦耐(大连)工程技术有限公司 | A kind of Production Process for Modified Pitch |
| CN206887030U (en) * | 2017-06-20 | 2018-01-16 | 中冶焦耐(大连)工程技术有限公司 | A kind of Existing in Improved Pitch Production System |
| CN210340778U (en) * | 2019-07-19 | 2020-04-17 | 中冶焦耐(大连)工程技术有限公司 | System for two cauldron pressurization production modified pitch of twin-furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110240917A (en) | 2019-09-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101289624B (en) | Process for producing moderate temperature modified bitumen by continuously pressurizing and hot-polymerizing at two stages connected in series | |
| CN110240917B (en) | System and process for producing modified asphalt by double-furnace double-kettle pressurization | |
| CN210340778U (en) | System for two cauldron pressurization production modified pitch of twin-furnace | |
| CN107057740B (en) | Modified asphalt production device | |
| CN110240918B (en) | System and process for producing modified asphalt by double-furnace double-kettle stripping flash evaporation | |
| CN107245346B (en) | Modified asphalt production process | |
| CN210560259U (en) | System for producing modified asphalt by double-furnace double-kettle stripping flash evaporation | |
| CN102980166B (en) | Steam-water circulating system utilizing waste heat of high-temperature calcined coke generated by pot calciner | |
| CN206887030U (en) | A kind of Existing in Improved Pitch Production System | |
| CN214571727U (en) | Modified asphalt production system adopting horizontal reaction kettle | |
| CN112973607A (en) | Continuous production device and process of chlormequat chloride | |
| CN218901838U (en) | Device for synthesizing nitromethane from sodium nitrite and dimethyl sulfate | |
| CN111234933A (en) | Device for producing biodiesel by continuous ester exchange of waste oil and fat | |
| CN211936936U (en) | Modified asphalt reaction kettle with side feeding and full flow discharging functions | |
| CN211946912U (en) | Gas is in same direction as circulation falling film cooling device | |
| CN210915939U (en) | Air oxidation device for preparing coal tar pitch with high softening point | |
| CN110143883B (en) | Hydrogenation reaction method | |
| CN211111803U (en) | Dimethyl phosphite apparatus for producing | |
| CN209872869U (en) | Modified asphalt production system | |
| CN110527539B (en) | Coal-based needle coke pretreatment device and process method | |
| CN111961495A (en) | Production process and system for modifying asphalt by multi-kettle series-connected tubular furnace heating method | |
| CN216427210U (en) | Modified asphalt production system | |
| CN206736190U (en) | A kind of waste boiler type catalytic gasification stove | |
| CN111961496A (en) | Production process and system for modifying asphalt by multi-reaction-kettle parallel tubular furnace heating method | |
| CN112745870A (en) | Modified asphalt production system and process adopting horizontal reaction kettle |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |