CN114540064A - Process and system for producing modified asphalt by combining direct heating kettle with modifying tower - Google Patents
Process and system for producing modified asphalt by combining direct heating kettle with modifying tower Download PDFInfo
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- 239000010426 asphalt Substances 0.000 title claims abstract description 245
- 238000010438 heat treatment Methods 0.000 title claims abstract description 75
- 238000000034 method Methods 0.000 title claims abstract description 57
- 238000006243 chemical reaction Methods 0.000 claims abstract description 141
- 238000012986 modification Methods 0.000 claims abstract description 25
- 230000004048 modification Effects 0.000 claims abstract description 25
- 238000006011 modification reaction Methods 0.000 claims abstract description 20
- 238000001816 cooling Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 58
- 239000007789 gas Substances 0.000 claims description 52
- 238000009833 condensation Methods 0.000 claims description 37
- 230000005494 condensation Effects 0.000 claims description 37
- 238000005406 washing Methods 0.000 claims description 19
- 238000001704 evaporation Methods 0.000 claims description 14
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000002407 reforming Methods 0.000 claims description 11
- 239000002737 fuel gas Substances 0.000 claims description 9
- 238000005086 pumping Methods 0.000 claims description 7
- 238000004821 distillation Methods 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 238000004939 coking Methods 0.000 abstract description 10
- 230000009286 beneficial effect Effects 0.000 abstract description 7
- 230000002349 favourable effect Effects 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 64
- 239000000047 product Substances 0.000 description 26
- 238000006068 polycondensation reaction Methods 0.000 description 10
- 239000002994 raw material Substances 0.000 description 8
- 239000011269 tar Substances 0.000 description 7
- 239000011280 coal tar Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000012545 processing Methods 0.000 description 6
- 239000011347 resin Substances 0.000 description 6
- 229920005989 resin Polymers 0.000 description 6
- 238000003860 storage Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000011295 pitch Substances 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000002715 modification method Methods 0.000 description 2
- 238000005580 one pot reaction Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000011300 coal pitch Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
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Classifications
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- 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
-
- 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
- C10C3/10—Melting
- C10C3/12—Devices therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28B—STEAM OR VAPOUR CONDENSERS
- F28B1/00—Condensers in which the steam or vapour is separate from the cooling medium by walls, e.g. surface condenser
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to a process and a system for producing modified asphalt by combining a direct heating kettle with a modifying tower.A medium-temperature asphalt is sent to the modifying tower for continuous thermal modification reaction after being subjected to modification reaction in 2 continuous direct heating reaction kettles; the temperature of the 2 continuous direct heating reaction kettles is 370-390 ℃, and the temperature of the modifying tower is 340-360 ℃; part of the modified asphalt from the modifying tower returns to the modifying tower for circulation, and the rest is sent out as a modified asphalt product. In the invention, the direct heating kettle adopts the cooling operation, thereby reducing the possibility of equipment and pipeline coking and prolonging the operation period of the asphalt modifying device; the modification tower adopts negative pressure operation, which is beneficial to the volatilization of light components of the asphalt and improves the softening point of the asphalt; part of the modified asphalt from the modifying tower returns to the internal circulation of the tower, which is favorable for adjusting the softening point of the modified asphalt product.
Description
Technical Field
The invention relates to the technical field of coal tar deep processing, in particular to a process and a system for producing modified asphalt by combining a direct heating kettle with a modifying tower.
Background
Along with the explosive development of the domestic coking industry, the yield of coal tar is increased year by year, the increase of the scale of the coal tar deep processing industry is also emphasized, how to effectively prolong the coal tar deep processing chain and increase the additional value of the coal tar deep processing product becomes a new exploration proposition in the industry, and the research direction of taking coal pitch as a carbon-based raw material is mainly focused. For coal tar deep processing enterprises, how to efficiently produce high-quality asphalt products is the key for seizing the market, obtaining effective profits and winning long-term development in the future.
At present, the typical production methods of modified asphalt at home and abroad mainly comprise a thermal polycondensation method and a vacuum flash evaporation method. The vacuum flash evaporation method is to vaporize medium-temperature asphalt under vacuum condition to increase the softening point and coke deposition amount of the asphalt, but the content of toluene insoluble substances and quinoline insoluble substances is less changed, so the method is not generally adopted to produce the modified asphalt. The thermal polycondensation method can be classified into a kettle-type heating method and a tube furnace heating method according to the heating manner; the method can be divided into three methods of negative pressure, normal pressure and pressurization according to the operation pressure, and the technological process is briefly introduced as follows:
1. french Litwin process
The French Litwin process is a double-furnace double-kettle and tubular furnace heating and pressurizing thermal polycondensation process.
The medium temperature pitch enters into 1# reaction kettle, to be modified, to generate beta resin through adjusting the temperature of the reaction kettle. And the asphalt at the bottom of the kettle is pumped out by a circulating pump, one part of the asphalt is sent to the No. 1 tubular furnace to be heated and then returned to the kettle, and the other part of the asphalt is sent to the inlet of the No. 2 tubular furnace to be mixed with the circulating asphalt of the No. 2 reaction kettle and then enter the No. 2 tubular furnace. Asphalt from the No. 1 reaction kettle continues to carry out modification reaction in the No. 2 reaction kettle, the temperature of the reaction kettle is adjusted to mainly generate alpha resin, the asphalt at the bottom of the reaction kettle is pumped out by a circulating pump, one part of the asphalt is sent to the No. 2 tube furnace to be heated and then returned to the reaction kettle, and the other part of the asphalt is sent to a stripping tower. And stripping the asphalt intermediate product subjected to the two-time modification reaction by oil gas and superheated steam at the top of the reaction kettle in a stripping tower to obtain a modified asphalt product, wherein the stripping tower is operated under normal pressure. Nitrogen is introduced into the two reaction kettles, and the modification reaction is pressurized operation.
The process is carried out in two steps, the generation amount of the beta-component and the alpha-component can be effectively controlled, the beta-resin is generated by the pressurized reaction, and the coking value is improved; the separation of asphalt and oil by steam stripping is favorable for the adjustment of softening point. The disadvantages are that: the pressurization method increases the reaction temperature, the asphalt is easy to coke, and the energy consumption is large. The stripping process separates the asphalt and oil products to produce a large amount of process wastewater.
2. German Uhde process
The German Uhde process is a single-furnace single-kettle and tubular furnace heating and negative pressure thermal polycondensation process.
The medium temperature asphalt of raw materials enters a reaction kettle, and a thermal polycondensation reaction is carried out in the reaction kettle to change the asphalt components. The asphalt at the bottom of the reaction kettle is pumped out by an asphalt circulating pump, most of the asphalt is sent to a heating furnace for circulating heating, and the small part of the asphalt is sent to an asphalt flash tank, and the softening point of the asphalt is further improved by the gas stripping of oil gas at the top of the reaction kettle, so that a qualified modified asphalt product is produced. The non-condensable gas after the oil gas at the top of the flash tank is condensed and cooled enters a vacuum system to provide negative pressure for the reaction kettle.
The process is characterized in that the asphalt modification process is completed in a negative pressure kettle, the process flow is short, the reaction temperature is lower, the coking is favorably reduced, and the energy consumption is reduced. But the modification reaction is finished in one kettle, the requirements on temperature and time control are higher, and the adjustable range of the product quality is narrower; the asphalt and the oil product are separated in the flash tank, and the obtained modified asphalt has a lower softening point.
3. Japanese JFE process
The production process of the modified pitch of the Japan JFE has no independent production unit, and only adds part of equipment in a tar distillation unit. The specific process flow is as follows: the top of the tar fractionating tower is connected with a vacuum system, heavy oil fraction is cut off at the side line, and asphalt at the bottom of the tower automatically flows into an asphalt storage tank and is subjected to thermal polycondensation reaction, so that the asphalt component is changed. The asphalt at the bottom of the storage tank is pumped out by an asphalt circulating pump and sent to a heating furnace, and the heated asphalt returns to a tar fractionating tower to provide heat required by distillation and modification. The modified asphalt product is pumped out by a pump at the bottom of the asphalt storage tank.
The process is characterized in that: the modification and the separation of the asphalt and the oil products are directly finished in the tar fractionating tower and the asphalt storage tank, and the process flow is shortest; the modification belongs to one-step reaction and is a negative pressure operation, which is beneficial to reducing coking and energy consumption. However, the disadvantages reflected by the practical operation are as follows: short residence time in the modification process, incomplete polycondensation, poor product quality and low content of beta-resin.
4. Continuous thermal modification method of direct heating kettle
The continuous thermal modification process system of the direct heating kettle is formed by connecting 2 or 3 asphalt reaction kettles in series. The medium temperature asphalt firstly enters a No. 1 reaction kettle to carry out thermal polycondensation reaction, and then automatically flows to a No. 2 reaction kettle to continue the thermal polycondensation reaction. And a heating furnace is arranged outside the reaction kettle, fuel gas is used for directly heating the asphalt in the reaction kettle to provide heat for thermal polycondensation, the temperature of the reaction kettle is controlled according to the quality requirement, and the modified asphalt is discharged from the bottom of the No. 2 reaction kettle to a modified asphalt intermediate tank after the modified asphalt is qualified in quality. And flash oil steam generated at the top of the reaction kettle flows into a flash oil groove after being condensed and cooled.
The process becomes the most widely applied modified asphalt production process in China at one time, and the technology is mature and reliable. But the treatment capacity is small, the production temperature is high, the asphalt is easy to coke, the pipeline is seriously blocked, and the system operation period is short.
5. Single-furnace double-kettle negative pressure modification process
Mixing the raw material asphalt with the circulating asphalt of the two reaction kettles, feeding the mixture into a heating furnace, heating the mixture to a certain temperature, feeding the mixture into a flash evaporation tank, and performing flash evaporation under negative pressure; the asphalt at the bottom of the flash tank flows into the No. 1 reaction kettle, and stays there for upgrading reaction. Pumping out asphalt at the bottom of the kettle by a # 1 circulating pump, and returning a part of the asphalt into the kettle in a self-circulation manner; the other part is sent to a No. 2 reaction kettle operated in series for continuous residence, and further modification reaction is carried out; and a part of the asphalt is mixed with the circulating asphalt of the No. 2 reaction kettle and the raw material asphalt and then enters a heating furnace. Pumping out the asphalt at the bottom of the No. 2 kettle by a No. 2 circulating pump, and returning a part of the asphalt to the kettle in a self-circulating manner; the other part is mixed with the 1# reaction kettle circulating asphalt and the raw material asphalt and then enters a heating furnace. And pumping the asphalt at the bottom of the No. 1 reaction kettle by an asphalt extraction pump, conveying the asphalt to a stripping tower, and stripping by superheated steam to obtain a modified asphalt product, wherein the stripping tower is operated under normal pressure. The flash tank is connected with a vacuum system to provide negative pressure for the reaction kettle.
The modification process of the process is operated under the condition of negative pressure, the reaction temperature is lower, and the coking is favorably reduced. Although two reaction kettles exist, the two kettles are operated in a cascade mode, the reaction still belongs to one-step reaction, and the requirements on temperature and time control are high; separating asphalt and oil products by a steam stripping method to generate a large amount of process wastewater; the raw material asphalt is flash evaporated before modification, and is more suitable for low-softening-point raw materials.
6. Double-furnace double-kettle negative pressure modification process
The raw material medium temperature asphalt is firstly mixed with the circulating asphalt of the post-furnace No. 1 reaction kettle, enters the No. 1 reaction kettle and stays in the reaction kettle for modification reaction, and the temperature is controlled to ensure that the beta-resin is mainly generated. And the asphalt at the bottom of the reaction kettle is pumped out by a # 1 circulating pump, one part of the asphalt is heated by a # 1 heating furnace and then returns to a # 1 reaction kettle, the other part of the asphalt is mixed with the circulating asphalt of the # 2 reaction kettle and then enters a # 2 tubular furnace, and the mixture enters a # 2 reaction kettle after being heated and is further subjected to a modification reaction. The temperature of the reaction kettle is adjusted to control the reaction kettle to mainly generate alpha-resin. The asphalt at the bottom of the kettle is pumped out by a No. 2 circulating pump, and one part of the asphalt is sent to a No. 2 tubular furnace to be heated and then returned to the kettle to provide heat required by polymerization and reaction; the other part is sent to a modifying tower, and the retention time is increased to separate the asphalt from the oil gas, so as to obtain a modified asphalt product. Oil gas at the tops of the 1# reaction kettle and the 2# reaction kettle is condensed and cooled and then enters a vacuum system to provide negative pressure for the two reaction kettles, and the modification tower is operated under normal pressure.
The modification reaction of the process is carried out in two steps, and the generation amount of beta-components and alpha-components can be effectively controlled; the modification process is operated under the condition of negative pressure, the reaction temperature is lower, and the coking is favorably reduced. The operation process does not need steam to participate, and process wastewater is not generated.
Disclosure of Invention
The invention provides a process and a system for producing modified asphalt by combining a direct heating kettle with a modifying tower, which realize continuous production of the modified asphalt; the direct heating kettle adopts the cooling operation, thereby reducing the possibility of equipment and pipeline coking and prolonging the operation period of the asphalt modifying device; the modification tower adopts negative pressure operation, which is beneficial to the volatilization of light components of the asphalt and improves the softening point of the asphalt; part of the modified asphalt from the modifying tower returns to the tower for circulation, which is beneficial to adjusting the softening point of the modified asphalt product.
In order to achieve the purpose, the invention adopts the following technical scheme:
a direct heating kettle combined with a modifying tower for producing modified asphalt, wherein medium-temperature asphalt is sent to the modifying tower for continuous thermal modification reaction after modification reaction is carried out in 2 continuous direct heating reaction kettles; the temperature of the 2 continuous direct heating reaction kettles is 370-390 ℃, and the temperature of the modifying tower is 340-360 ℃; returning part of the modified asphalt from the modifying tower to the modifying tower for internal circulation, and delivering the rest of the modified asphalt as a modified asphalt product; the top of the modifying tower adopts negative pressure operation, and vacuum tail gas is sent to a reaction kettle heating furnace by a vacuum unit for incineration treatment.
A process for producing modified asphalt by combining a direct heating kettle with a modifying tower comprises the following steps:
1) direct kettle type heating modification;
liquid medium-temperature asphalt from a tar distillation unit is conveyed into a first reaction kettle, when the first reaction kettle is filled, the liquid asphalt discharged from the bottom of the first reaction kettle flows into a second reaction kettle, and the first reaction kettle and the second reaction kettle are directly heated by adopting fuel gas through a reaction kettle heating furnace; controlling the reaction temperature according to the quality requirement of the finished product, discharging the liquid asphalt reaching the set quality target from the bottom of the second reaction kettle to a modified asphalt intermediate tank, and pumping the liquid asphalt to a modified tower through a liquid asphalt pump;
2) modifying in a modifying tower;
the liquid level of the modified asphalt intermediate tank is ensured to be constant by adjusting the flow of the liquid asphalt entering the modified tower; the modified asphalt continues to carry out thermal modification reaction in the modification tower; pumping out the modified asphalt at the bottom of the modified tower by a modified asphalt circulating pump, returning a part of the modified asphalt to the modified tower for circulation, and sending out the rest of the modified asphalt as a modified asphalt product;
3) oil gas treatment;
the top of the reforming tower adopts negative pressure operation, flash evaporation oil vapor at the top of the reforming tower enters an oil gas condensation cooler, after circulating water is condensed and cooled, gas phase enters a vacuum exhaust condensation cooler for further cooling, and tail gas of the vacuum exhaust condensation cooler is sent to a reaction kettle heating furnace by a vacuum unit for incineration treatment; the liquid flash oil generated by the oil gas condensation cooler and the vacuum exhaust condensation cooler automatically flows to the emptying groove and is periodically pumped out by the flash oil pump.
And new washing oil is supplemented into the vacuum unit through the oil washing groove, and waste washing oil is discharged into the emptying groove.
A system for producing modified asphalt by combining a direct heating kettle with a modifying tower comprises a first reaction kettle, a second reaction kettle, a modified asphalt intermediate tank, a modifying tower, an oil gas condensing cooler, a vacuum exhaust condensing cooler, a vacuum unit and an emptying tank; the outside of the first reaction kettle and the outside of the second reaction kettle are respectively provided with a reaction kettle heating furnace; the upper part of the first reaction kettle is provided with a medium temperature asphalt inlet, a liquid asphalt outlet at the bottom of the first reaction kettle is connected with a liquid asphalt inlet at the upper part of the second reaction kettle, and a hydraulic asphalt outlet at the bottom of the second reaction kettle is connected with a modified asphalt intermediate tank; a liquid asphalt outlet of the modified asphalt intermediate tank is connected with a liquid asphalt inlet at the upper part of the modified tower through a liquid asphalt pipeline, and the liquid asphalt pipeline is provided with a liquid asphalt pump; the modified asphalt outlet at the bottom of the modified tower is connected with the circulating asphalt inlet at the upper part of the modified tower through an asphalt circulating pipeline, and the asphalt circulating pipeline is provided with a modified asphalt circulating pump and a modified asphalt product outlet; the top of the reforming tower is provided with a flash evaporation oil gas outlet, and the reforming tower is sequentially connected with an oil gas condensation cooler, a vacuum exhaust condensation cooler and a vacuum unit through a flash evaporation oil gas pipeline, wherein a tail gas outlet of the vacuum unit is connected with a tail gas inlet of a reaction kettle heating furnace, and a fuel gas inlet is additionally arranged outside the reaction kettle heating furnace; the oil washing inlet of the vacuum unit is connected with the oil washing tank, and the liquid phase outlet of the oil gas condensation cooler, the liquid phase outlet of the vacuum exhaust condensation cooler and the oil washing outlet of the vacuum unit are respectively connected with the inlet of the emptying tank; the outlet of the emptying groove is connected with a flash oil pipeline, and a flash oil pump is arranged on the flash oil pipeline.
Stirring devices are arranged in the first reaction kettle and the second reaction kettle.
Compared with the prior art, the invention has the beneficial effects that:
1) the process flow is simple and easy to implement, and the overall operation energy consumption is low;
2) the residual heat of the asphalt is utilized to carry out thermal modification reaction without supplementing extra heat;
3) the modification tower adopts negative pressure operation, which is beneficial to the volatilization of light components of the asphalt and improves the softening point of the asphalt;
4) part of the modified asphalt from the modifying tower returns to the tower for circulation, which is beneficial to adjusting the softening point of the modified asphalt product;
5) the modification tower and the vacuum unit are arranged, so that the retention time of the liquid asphalt is prolonged, the operating temperature of the reaction kettle is greatly reduced, the possibility of equipment and pipeline coking is reduced, the operation period of the asphalt modification device is prolonged, and the adjustable range of the product quality is wide;
6) the vacuum tail gas is sent to a heating furnace of the reaction kettle for incineration treatment, so that the aim of environmental protection is fulfilled and the consumption of fuel gas is reduced.
Drawings
FIG. 1 is a schematic structural diagram of a system for producing modified asphalt by using a direct heating kettle combined with a modifying tower.
In the figure: 1. a first reaction kettle 2, a second reaction kettle 3, a reaction kettle heating furnace 4, a modified asphalt intermediate tank 5, a modified tower 6, an oil gas condensation cooler 7, a vacuum exhaust condensation cooler 8, a vacuum unit 9, an emptying tank 10, an oil washing tank 11, a liquid asphalt pump 12, a modified asphalt circulating pump 13, a flash oil pump 13
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
the invention relates to a process for producing modified asphalt by combining a direct heating kettle and a modifying tower, wherein medium-temperature asphalt is sent to the modifying tower for continuous thermal modification reaction after modification reaction is carried out in 2 continuous direct heating reaction kettles; the temperature of the 2 continuous direct heating reaction kettles is 370-390 ℃, and the temperature of the modifying tower is 340-360 ℃; returning part of the modified asphalt from the modifying tower to the modifying tower for internal circulation, and delivering the rest of the modified asphalt as a modified asphalt product; the top of the modifying tower adopts negative pressure operation, and vacuum tail gas is sent to a reaction kettle heating furnace by a vacuum unit for incineration treatment.
As shown in figure 1, the process for producing the modified asphalt by combining the direct heating kettle with the modifying tower comprises the following steps:
1) direct kettle type heating modification;
liquid medium-temperature asphalt from a tar distillation unit is conveyed into a first reaction kettle 1, when the first reaction kettle 1 is filled, the liquid asphalt discharged from the bottom of the first reaction kettle flows into a second reaction kettle 2, and the first reaction kettle 1 and the second reaction kettle 2 are directly heated by adopting fuel gas through a reaction kettle heating furnace 3; controlling the reaction temperature according to the quality requirement of the finished product, discharging the liquid asphalt reaching the set quality target from the bottom of the second reaction kettle to a modified asphalt intermediate tank 4, and conveying the liquid asphalt to a modified tower 5 through a liquid asphalt pump 11;
2) modifying in a modifying tower;
the liquid level of the modified asphalt intermediate tank 4 is ensured to be constant by adjusting the flow of the liquid asphalt entering the modifying tower 5; the modified asphalt continues to carry out thermal modification reaction in the modifying tower 5; the modified asphalt at the bottom of the modifying tower 5 is pumped out by a modified asphalt circulating pump 12, a part of the modified asphalt returns to the modifying tower 5 for circulation, and the rest of the modified asphalt is sent out as a modified asphalt product;
3) oil gas treatment;
the top of the reforming tower adopts negative pressure operation, flash evaporation oil vapor at the top of the reforming tower 5 enters an oil gas condensation cooler 6, after being condensed and cooled by circulating water, a gas phase enters a vacuum exhaust condensation cooler 7 for further cooling, and tail gas of the vacuum exhaust condensation cooler 7 is sent to a reaction kettle heating furnace 3 by a vacuum unit 8 for incineration treatment; the liquid flash oil generated by the oil gas condensation cooler 6 and the vacuum exhaust condensation cooler 7 automatically flows to the emptying tank 9 and is sent out by the flash oil pump 13 periodically.
Fresh washing oil is supplemented into the vacuum unit 8 through the washing oil groove 11, and waste washing oil is discharged into the emptying groove 9.
A system for producing modified asphalt by a direct heating kettle combined modification tower comprises a first reaction kettle 1, a second reaction kettle 2, a modified asphalt intermediate tank 4, a modification tower 5, an oil gas condensation cooler 6, a vacuum exhaust condensation cooler 7, a vacuum unit 8 and an emptying tank 9; the outside of the first reaction kettle 1 and the outside of the second reaction kettle 2 are respectively provided with a reaction kettle heating furnace 3; the upper part of the first reaction kettle 1 is provided with a medium-temperature asphalt inlet, a liquid asphalt outlet at the bottom of the first reaction kettle 1 is connected with a liquid asphalt inlet at the upper part of the second reaction kettle 2, and a hydraulic asphalt outlet at the bottom of the second reaction kettle 2 is connected with a modified asphalt intermediate tank 4; a liquid asphalt outlet of the modified asphalt intermediate tank 4 is connected with a liquid asphalt inlet at the upper part of the modified tower 5 through a liquid asphalt pipeline, and the liquid asphalt pipeline is provided with a liquid asphalt pump 11; the modified asphalt outlet at the bottom of the modifying tower 5 is connected with the circulating asphalt inlet at the upper part of the modifying tower 5 through an asphalt circulating pipeline, and the asphalt circulating pipeline is provided with a modified asphalt circulating pump 12 and a modified asphalt product outlet; the top of the upgrading tower 5 is provided with a flash evaporation oil gas outlet, an oil gas condensation cooler 6, a vacuum exhaust condensation cooler 7 and a vacuum unit 8 are sequentially connected through a flash evaporation oil gas pipeline, a tail gas outlet of the vacuum unit 8 is connected with a tail gas inlet of the reaction kettle heating furnace 3, and the reaction kettle heating furnace 3 is additionally provided with a fuel gas inlet; a washing oil inlet of the vacuum unit 8 is connected with a washing oil tank 10, and a liquid phase outlet of the oil gas condensation cooler 6, a liquid phase outlet of the vacuum exhaust condensation cooler 7 and a washing oil outlet of the vacuum unit 8 are respectively connected with an inlet of the emptying tank 9; the outlet of the emptying groove 9 is connected with a flash oil pipeline, and a flash oil pump 13 is arranged on the flash oil pipeline.
Stirring devices are arranged in the first reaction kettle 1 and the second reaction kettle 2.
The process for producing the modified asphalt by the direct heating kettle combined modifying tower is improved on the basis of the existing direct heating kettle continuous thermal modifying method, and the modifying tower and the vacuum unit are arranged, so that the retention time of the liquid asphalt is prolonged, and the operating temperature of the reaction kettle is greatly reduced (from the conventional temperature of over 400 ℃ to 370-390 ℃), thereby effectively reducing the possibility of equipment and pipeline coking, prolonging the operating period of the modified asphalt device, improving the processing capacity and widening the adjustable range of the product quality. The operating parameters for the two processes are compared as shown in the following table:
| process parameters | Continuous thermal modification method of direct heating kettle | The invention is as describedProcess for producing a composite material |
| Temperature of reforming | Not lower than 400 DEG C | 370～385℃ |
| Residence time of asphalt | About 8h | About 16h |
| Range of asphalt softening point adjustment | 100～112℃ | 100～125℃ |
| Production cycle | About 20 days | About 45 days |
The following examples are carried out on the premise of the technical scheme of the invention, and detailed embodiments and specific operation processes are given, but the scope of the invention is not limited to the following examples.
[ examples ] A
As shown in fig. 1, in this embodiment, the process for producing modified asphalt by using a direct-heating kettle combined with a modifying tower includes the following steps:
1) direct kettle type heating modification
The medium temperature pitch that comes by tar distillation unit is sent to first reation kettle 1 in, and when first reation kettle 1 filled up, in the liquid pitch of discharging flows into second reation kettle 2 from first reation kettle bottom, 2 reation kettle all used fuel gas through reation kettle heating furnace 3 direct heating. The temperature is controlled according to the quality requirement, and the temperature in 2 reaction kettles is controlled at 385 ℃. After the set quality target is reached, the liquid asphalt is discharged from the bottom of the second reaction kettle to the modified asphalt intermediate tank 4, and then is sent to the modified tower 5 through the liquid asphalt pump 11.
2) Modifying tower for modifying
When the liquid asphalt in the modified asphalt intermediate tank 4 is sent to the modifying tower 5 through the liquid asphalt pump 11, the liquid level of the modified asphalt intermediate tank 4 is adjusted by controlling the flow rate of the liquid asphalt so as to keep the liquid level constant. The liquid asphalt is continuously subjected to thermal upgrading reaction in the upgrading tower 5, the temperature in the upgrading tower 5 is controlled to be 350 ℃, the upgraded asphalt at the bottom of the upgrading tower 5 is pumped out by the upgraded asphalt circulating pump 12, a part of the upgraded asphalt is returned to the upgrading tower 5 for circulation, and the rest of the upgraded asphalt is sent out as an upgraded asphalt product.
3) Oil and gas treatment
The top of the upgrading tower 5 is maintained in negative pressure operation, and the vacuum degree is maintained at 75 kPa. The flash evaporation oil vapor at the top of the modification tower 5 enters an oil gas condensation cooler 6, after condensation and cooling by circulating water, the vapor phase enters a vacuum exhaust condensation cooler 7 for further cooling, and the tail gas of the vacuum exhaust condensation cooler 7 is sent to the reaction kettle heating furnace 3 by a vacuum unit 8 for incineration treatment. The washing oil required by the vacuum unit 8 is supplemented by a washing oil storage tank 10, and the waste washing oil is discharged into an emptying tank 9.
The liquid flash oil generated by the oil gas condensation cooler 6 and the vacuum exhaust condensation cooler 7 automatically flows to the emptying tank 9 and is sent out by the flash oil pump 13 periodically.
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 (5)
1. A process for producing modified asphalt by combining a direct heating kettle with a modifying tower is characterized in that medium-temperature asphalt is sent to the modifying tower for continuous thermal modification reaction after modification reaction is carried out in 2 continuous direct heating reaction kettles; the temperature of the 2 continuous direct heating reaction kettles is 370-390 ℃, and the temperature of the modifying tower is 340-360 ℃; returning part of the modified asphalt from the modifying tower to the modifying tower for internal circulation, and delivering the rest of the modified asphalt as a modified asphalt product; the top of the modifying tower is operated under negative pressure, and vacuum tail gas is sent to a reaction kettle heating furnace by a vacuum unit for incineration treatment.
2. The process of claim 1 for producing upgraded asphalt by using a direct-heating kettle combined upgrading tower, which comprises the following steps:
1) direct kettle type heating modification;
liquid medium-temperature asphalt from a tar distillation unit is conveyed into a first reaction kettle, when the first reaction kettle is filled, the liquid asphalt discharged from the bottom of the first reaction kettle flows into a second reaction kettle, and the first reaction kettle and the second reaction kettle are directly heated by adopting fuel gas through a reaction kettle heating furnace; controlling the reaction temperature according to the quality requirement of the finished product, discharging the liquid asphalt reaching the set quality target from the bottom of the second reaction kettle to a modified asphalt intermediate tank, and pumping the liquid asphalt to a modified tower through a liquid asphalt pump;
2) modifying in a modifying tower;
the liquid level of the modified asphalt intermediate tank is ensured to be constant by adjusting the flow of the liquid asphalt entering the modified tower; the modified asphalt continues to carry out thermal modification reaction in the modifying tower; pumping out the modified asphalt at the bottom of the modified tower by a modified asphalt circulating pump, returning a part of the modified asphalt to the modified tower for circulation, and sending out the rest of the modified asphalt as a modified asphalt product;
3) oil gas treatment;
the top of the reforming tower adopts negative pressure operation, flash evaporation oil vapor at the top of the reforming tower enters an oil gas condensation cooler, after circulating water is condensed and cooled, gas phase enters a vacuum exhaust condensation cooler for further cooling, and tail gas of the vacuum exhaust condensation cooler is sent to a reaction kettle heating furnace by a vacuum unit for incineration treatment; the liquid flash oil generated by the oil gas condensation cooler and the vacuum exhaust condensation cooler automatically flows to the emptying groove and is periodically pumped out by the flash oil pump.
3. The process for producing modified asphalt by using the direct heating kettle combined with the modifying tower as claimed in claim 2, wherein new wash oil is supplied to the vacuum unit through the wash oil tank, and waste wash oil is discharged to the emptying tank.
4. The system for producing the modified asphalt by combining the direct heating kettle with the modifying tower for realizing the process of claims 1-3 is characterized by comprising a first reaction kettle, a second reaction kettle, a modified asphalt middle tank, a modifying tower, an oil gas condensing cooler, a vacuum exhaust condensing cooler, a vacuum unit and an emptying tank; the outside of the first reaction kettle and the outside of the second reaction kettle are respectively provided with a reaction kettle heating furnace; the upper part of the first reaction kettle is provided with a medium temperature asphalt inlet, a liquid asphalt outlet at the bottom of the first reaction kettle is connected with a liquid asphalt inlet at the upper part of the second reaction kettle, and a hydraulic asphalt outlet at the bottom of the second reaction kettle is connected with a modified asphalt intermediate tank; a liquid asphalt outlet of the modified asphalt intermediate tank is connected with a liquid asphalt inlet at the upper part of the modified tower through a liquid asphalt pipeline, and the liquid asphalt pipeline is provided with a liquid asphalt pump; the modified asphalt outlet at the bottom of the modified tower is connected with the circulating asphalt inlet at the upper part of the modified tower through an asphalt circulating pipeline, and the asphalt circulating pipeline is provided with a modified asphalt circulating pump and a modified asphalt product outlet; the top of the reforming tower is provided with a flash evaporation oil gas outlet, and the reforming tower is sequentially connected with an oil gas condensation cooler, a vacuum exhaust condensation cooler and a vacuum unit through a flash evaporation oil gas pipeline, wherein a tail gas outlet of the vacuum unit is connected with a tail gas inlet of a reaction kettle heating furnace, and a fuel gas inlet is additionally arranged outside the reaction kettle heating furnace; the oil washing inlet of the vacuum unit is connected with the oil washing tank, and the liquid phase outlet of the oil gas condensation cooler, the liquid phase outlet of the vacuum exhaust condensation cooler and the oil washing outlet of the vacuum unit are respectively connected with the inlet of the emptying tank; the outlet of the emptying groove is connected with a flash oil pipeline, and a flash oil pump is arranged on the flash oil pipeline.
5. The system for producing the modified asphalt by the direct-heating kettle combined modifying tower as claimed in claim 4, wherein stirring devices are arranged in the first reaction kettle and the second reaction kettle.
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| CN202210211811.0A CN114540064A (en) | 2022-03-04 | 2022-03-04 | Process and system for producing modified asphalt by combining direct heating kettle with modifying tower |
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| CN202210211811.0A CN114540064A (en) | 2022-03-04 | 2022-03-04 | Process and system for producing modified asphalt by combining direct heating kettle with modifying tower |
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| GB616730A (en) * | 1946-09-10 | 1949-01-26 | Thomas Owston Wilton | Improvements in the production of hard pitch and oils from medium soft coal tar pitch |
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| CN112342048A (en) * | 2020-11-26 | 2021-02-09 | 中冶焦耐(大连)工程技术有限公司 | Tubular furnace heating method modified asphalt production system and cleaning process thereof |
| CN217103726U (en) * | 2022-03-04 | 2022-08-02 | 中冶焦耐(大连)工程技术有限公司 | System for producing modified asphalt by combining direct heating kettle with modification tower |
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Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB616730A (en) * | 1946-09-10 | 1949-01-26 | Thomas Owston Wilton | Improvements in the production of hard pitch and oils from medium soft coal tar pitch |
| CN201386075Y (en) * | 2009-03-30 | 2010-01-20 | 旭阳控股有限公司 | Multi-variety asphalt production device |
| CN103865556A (en) * | 2012-12-14 | 2014-06-18 | 上海宝钢化工有限公司 | Device and method for producing mesophase-free medium-temperature modified asphalt |
| CA2915898A1 (en) * | 2015-12-21 | 2017-06-21 | Boleslaw Ignasiak (Les) | An integrated method for in-situ recovering and upgrading bitumen/heavy oil to distillable liquids and generating super clean diesel fuel and electric power |
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| 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 |
| CN112342048A (en) * | 2020-11-26 | 2021-02-09 | 中冶焦耐(大连)工程技术有限公司 | Tubular furnace heating method modified asphalt production system and cleaning process thereof |
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