CN107057740B - Modified asphalt production device - Google Patents
Modified asphalt production device Download PDFInfo
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- CN107057740B CN107057740B CN201710467653.4A CN201710467653A CN107057740B CN 107057740 B CN107057740 B CN 107057740B CN 201710467653 A CN201710467653 A CN 201710467653A CN 107057740 B CN107057740 B CN 107057740B
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- asphalt
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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
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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
- C10C3/06—Working-up pitch, asphalt, bitumen by distillation
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- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Working-Up Tar And Pitch (AREA)
Abstract
The invention relates to a modified asphalt production device.A raw material asphalt conveying pipeline is connected with an asphalt inlet of a flash tower at the upper part of a flash evaporation modification reaction kettle, and an oil gas production outlet of the flash tower is connected with an oil gas condensation cooler; the asphalt outlet of the lower reaction kettle is connected with the furnace tube inlet of the first tubular heating furnace, and the furnace tube outlet of the first tubular heating furnace is connected with the asphalt inlet of the secondary modification reaction kettle; one path of the asphalt outlet of the secondary modification reaction kettle is connected with an asphalt conveying pipeline I at the upstream of the first connecting pipe type heating furnace, and the other path of the asphalt outlet of the secondary modification reaction kettle is connected with an asphalt inlet of the fractionating tower; an oil gas extraction port of the secondary modification reaction kettle is connected with an oil gas inlet at the lower part of the fractionating tower; the oil gas extraction outlet of the fractionating tower is connected with an oil gas condensation cooler, and the modified asphalt extraction outlet of the fractionating tower is connected with a modified asphalt delivery pipeline. The invention adopts a double-kettle two-step reaction method, can effectively control the generation amount of alpha-components and beta-components, and has controllable product quality; the process is simple, feasible, energy-saving and environment-friendly, and is suitable for various asphalt raw materials.
Description
Technical Field
The invention relates to the technical field of asphalt production, in particular to an energy-saving and environment-friendly modified asphalt production device suitable for various asphalt raw materials.
Background
About 50% -60% of asphalt is generally generated in the coal tar processing process, which belongs to a bulk product of tar processing, and the larger the processing scale is, the more the asphalt yield is. The modified asphalt is the main downstream product of the existing asphalt and is mainly used for producing prebaked anodes in the electrolytic aluminum industry to prepare battery rods or electrode binders.
At present, the kettle type thermal polycondensation process is mostly adopted for producing modified asphalt in China. The process uses medium-temperature asphalt as a raw material, and achieves the purpose of asphalt modification by controlling certain reaction residence time and proper reaction temperature in a reaction kettle directly heated by a heating furnace. Because the heating surface is the outer surface of the reaction kettle, in order to achieve good mass and heat transfer effects, a stirrer needs to be arranged in the reaction kettle, so that the volume of the reaction kettle is limited, and therefore, in order to achieve proper reaction time, two to three kettles are generally required to be connected in series for operation. In addition, the reforming reaction is generally carried out at atmospheric pressure due to the problem of sealing of the stirrer at high temperatures. The kettle type thermal polycondensation process has short process flow and simple and easy process; the method has the disadvantages that the equipment and the pipeline are easy to coke, the reaction controllability is poor, the operation is inconvenient, the heating in the reaction kettle is uneven, the product quality is poor, the design capability of each system is limited due to the volume limitation of the kettle.
In order to improve the defects of the process, a modified asphalt process heated by a tubular furnace appears, such as a pressurized double-furnace double-kettle stripping flash process introduced from France, a domestic single-furnace single-kettle stripping flash process and the like.
The pressurized double-kettle double-furnace steam stripping flash evaporation process uses medium-temperature asphalt as a raw material, asphalt is heated in a tubular heating furnace, and then reaction is carried out in a reaction kettle. The reaction is carried out in two steps and is a pressurized reaction, and flash steam stripping is carried out in a stripping tower after the reaction. The process has the advantages that two-step reaction is adopted, the generation amount of alpha-components and beta-components can be effectively controlled, and the product quality is controllable; the pressurized reaction is beneficial to the generation of beta-resin, and the coking value is improved; the asphalt and the oil product are separated by a steam stripping method, which is beneficial to the adjustment of the softening point; the disadvantages are that asphalt is easy to coke during the pressure modification reaction and the energy consumption is high; the stripping process for separating asphalt and oil also produces a large amount of process wastewater.
The single-furnace single-kettle stripping flash 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, and the reaction is completed in one step and is a pressurized reaction. After the reaction, the reaction product is flash stripped in a stripping tower. The process has the advantages of one-step reaction, short process flow, relatively low energy consumption, pressurized reaction favorable for the generation of beta-resin and high coking value. The disadvantages that the one-step reaction has higher control requirements on temperature and time, and the product quality is difficult to control; the use of stripping to separate asphalt from oil also produces a large amount of process wastewater.
In conclusion, at present, no modified asphalt production device which is perfect, suitable for various asphalt raw materials, energy-saving, environment-friendly and excellent in product quality exists in China.
Disclosure of Invention
The invention provides a modified asphalt production device, which adopts a double-kettle two-step reaction method, can effectively control the generation amount of alpha-components and beta-components, and has controllable product quality; the process is simple, feasible, energy-saving and environment-friendly, and is suitable for various asphalt raw materials.
In order to achieve the purpose, the invention adopts the following technical scheme:
a modified asphalt production device comprises a flash evaporation modified reaction kettle, a tubular heating furnace I, a secondary modified reaction kettle and a fractionating tower; the flash evaporation modification reaction kettle consists of a flash evaporation tower at the upper part and a reaction kettle at the lower part which are communicated with each other, an asphalt inlet of the flash evaporation tower is connected with a raw material asphalt conveying pipeline, and an oil gas extraction outlet at the top part of the flash evaporation tower is connected with an oil gas condensation cooler; an asphalt outlet at the bottom of the reaction kettle is connected with a furnace tube inlet of the first tubular heating furnace, and a furnace tube outlet of the first tubular heating furnace is connected with an asphalt inlet at the upper part of the secondary modification reaction kettle; the bottom asphalt outlet of the secondary modification reaction kettle is divided into two paths, one path is connected with an asphalt inlet in the middle of the fractionating tower through an asphalt conveying pipeline II, and the other path is connected with an asphalt conveying pipeline I on the upstream of a furnace pipe inlet of the first heating furnace of the tubular heating furnace; an oil gas extraction port at the top of the secondary modification reaction kettle is connected with an oil gas inlet at the lower part of the fractionating tower; the oil gas extraction outlet at the top of the fractionating tower is connected with an oil gas condensation cooler, and the modified asphalt extraction outlet at the bottom of the fractionating tower is connected with a modified asphalt delivery pipeline.
The device also comprises a second tubular heating furnace, wherein a furnace tube inlet of the second tubular heating furnace is connected with the first asphalt conveying pipeline, and a furnace tube outlet is connected with a raw material asphalt conveying pipeline at the upstream of the asphalt inlet of the flash tower at the upper part of the flash modification reaction kettle.
And the asphalt conveying pipeline I and the asphalt conveying pipeline II are respectively provided with an asphalt circulating pump.
And the modified asphalt delivery pipeline is provided with a modified asphalt pump and a modified asphalt cooler.
The upper part of the fractionating tower is provided with a side line flash oil circulating pipeline, and the flash oil circulating pipeline is provided with a flash oil cooler and a circulating flash oil pump.
An oil gas outlet of the oil gas condensation cooler is connected with an oil-water separation tank, a flash oil outlet of the oil-water separation tank is connected with a flash oil circulating pipeline at the lateral line of the fractionating tower, and a non-condensable gas outlet of the oil-water separation tank is connected with a vacuum system.
Compared with the prior art, the invention has the beneficial effects that:
1) The process flow is short and simple and feasible;
2) The negative pressure modification operation is adopted, so that the reaction temperature is reduced, and the possibility of coking of equipment and pipelines can be effectively reduced;
3) By controlling the reaction time and the reaction temperature, the beta-resin content and the coking value of the asphalt product can be effectively improved, so that the quality of the modified asphalt product is controllable;
4) The double-kettle two-step reaction is adopted, and the beta-modification and the alpha-modification are respectively carried out in 2 reaction kettles, so that the control flexibility of the modification reaction is ensured, and the requirement on product quality diversification can be met;
5) The flash evaporation function is added before the first step of polycondensation reaction, so that the requirement of raw material diversification can be met;
6) The process of separating oil products and asphalt by using the fractionating tower can improve the separation efficiency; meanwhile, a large amount of process wastewater is avoided, and the energy is saved and the environment is protected;
7) Through carrying out rational layout and design to the tube furnace, can realize single stove double cauldron technology.
Drawings
FIG. 1 is a schematic view of the structure of an apparatus for producing a modified pitch according to the present invention.
In the figure: 1. flash evaporation modification reaction kettle 2, secondary modification reaction kettle 31, tubular heating furnace I32, tubular heating furnace II 4, asphalt circulating pump 5, fractionating tower 6, modified asphalt pump 7, modified asphalt cooler 8, oil gas condensation cooler 9, oil-water separation tank 10, circulating flash evaporation oil pump 11 and flash evaporation oil cooler
A. Raw material asphalt B, modified asphalt C, non-condensable gas D and flash oil
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1, the modified asphalt production device of the present invention comprises a flash evaporation modification reaction kettle 1, a first tubular heating furnace 31, a second modification reaction kettle 2 and a fractionating tower 5; the flash evaporation modification reaction kettle 1 consists of a flash evaporation tower at the upper part and a reaction kettle at the lower part which are communicated with each other, an asphalt inlet of the flash evaporation tower is connected with a raw material asphalt conveying pipeline, and an oil gas extraction outlet at the top part of the flash evaporation tower is connected with an oil gas condensation cooler 8; an asphalt outlet at the bottom of the reaction kettle is connected with a furnace tube inlet of a first tubular heating furnace 31, and a furnace tube outlet of the first tubular heating furnace 31 is connected with an asphalt inlet at the upper part of the secondary modification reaction kettle 2; the bottom asphalt outlet of the secondary modification reaction kettle 2 is divided into two paths, one path is connected with the asphalt inlet in the middle of the fractionating tower 5 through an asphalt conveying pipeline II, and the other path is connected with an asphalt conveying pipeline I on the upstream of the furnace tube inlet of the tubular heating furnace I31; an oil gas extraction outlet at the top of the secondary modification reaction kettle 2 is connected with an oil gas inlet at the lower part of the fractionating tower 5; an oil gas extraction outlet at the top of the fractionating tower 5 is connected with an oil gas condensation cooler 8, and a modified asphalt extraction outlet at the bottom of the fractionating tower 5 is connected with a modified asphalt delivery pipeline.
The device also comprises a second tubular heating furnace 32, wherein a furnace tube inlet of the second tubular heating furnace 32 is connected with the first asphalt conveying pipeline, and a furnace tube outlet is connected with a raw material asphalt conveying pipeline at the upstream of the asphalt inlet of the flash tower at the upper part of the flash evaporation modification reaction kettle 1.
And the asphalt conveying pipeline I and the asphalt conveying pipeline II are respectively provided with an asphalt circulating pump 4.
And the modified asphalt delivery pipeline is provided with a modified asphalt pump 6 and a modified asphalt cooler 7.
The upper part of the fractionating tower 5 is provided with a side line flash oil circulating pipeline, and the flash oil circulating pipeline is provided with a flash oil cooler 11 and a circulating flash oil pump 10.
An oil gas outlet of the oil gas condensation cooler 8 is connected with an oil-water separation tank 9, a flash oil outlet of the oil-water separation tank 9 is connected with a flash oil circulating pipeline at the lateral line of the fractionating tower 5, and a non-condensable gas outlet of the oil-water separation tank 9 is connected with a vacuum system.
The raw material asphalt A is firstly mixed with the outlet asphalt of the second tubular heating furnace 32 and then enters a flash tower at the top of the flash modification reaction kettle 1 together, and the flash-modified asphalt falls into a reaction kettle at the lower part of the flash modification reaction kettle 1 and is subjected to modification reaction; the temperature in the reaction kettle is controlled to be 330-400 ℃ during the modification reaction, and the asphalt mainly generates beta-modification reaction;
the light oil product flashed in the upper flash tower and the reaction gas cracked in the lower reaction kettle transfer mass and heat in the flash tower, the heavy oil falls into the reaction kettle to continue to carry out the modification reaction, the light oil product leaves from the top of the flash tower and enters an oil gas condensation cooler 8, the cooled light oil product is collected as flash oil D, and the non-condensable gas C enters a vacuum system to ensure that the modification reaction is carried out under negative pressure;
most of the asphalt sent out from the bottom of the flash evaporation modification reaction kettle 1 enters a second tubular heating furnace 32 for circular heating, and the other small part of the asphalt is firstly mixed with the asphalt at the bottom of the second modification reaction kettle, then enters a first tubular heating furnace 31 for heating, and then enters a second modification reaction kettle 2; the temperature in the secondary modification reaction kettle 2 is controlled to be 350-420 ℃, and the asphalt mainly generates alpha-modification reaction; most of the asphalt at the bottom of the secondary modification reaction kettle 2 is sent to a first tubular heating furnace 31 for circular heating, and the small part is sent to a fractionating tower 5; pyrolysis gas at the top of the secondary upgrading reaction kettle also enters the fractionating tower 5;
the asphalt after two times of modification is separated from the oil product in a fractionating tower 5; the light oil product leaves from the top of the tower and enters an oil gas condensation cooler 8, the cooled light oil product is collected as flash oil D, and non-condensable gas C enters a vacuum system so as to ensure that the modification reaction in the secondary modification reaction kettle 2 and the fractionation process in the fractionating tower 5 are also carried out under negative pressure; after the flash oil D extracted from the side line of the fractionating tower 5 is cooled, one part of the flash oil D is sent out as a flash oil product, the rest is sent to the top of the fractionating tower to be used as reflux, and the modified asphalt B is extracted from the bottom of the fractionating tower.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (1)
1. A modified asphalt production device is characterized by comprising a flash evaporation modified reaction kettle, a tubular heating furnace I, a secondary modified reaction kettle and a fractionating tower; the flash evaporation modification reaction kettle consists of a flash evaporation tower at the upper part and a reaction kettle at the lower part which are communicated with each other, an asphalt inlet of the flash evaporation tower is connected with a raw material asphalt conveying pipeline, and an oil gas extraction outlet at the top part of the flash evaporation tower is connected with an oil gas condensation cooler; an asphalt outlet at the bottom of the reaction kettle is connected with a furnace tube inlet of the first tubular heating furnace, and a furnace tube outlet of the first tubular heating furnace is connected with an asphalt inlet at the upper part of the secondary modification reaction kettle; the bottom asphalt outlet of the secondary modification reaction kettle is divided into two paths, one path is connected with an asphalt inlet in the middle of the fractionating tower through an asphalt conveying pipeline II, and the other path is connected with an asphalt conveying pipeline I at the upstream of the furnace pipe inlet of the tubular heating furnace I; an oil gas extraction outlet at the top of the secondary modification reaction kettle is connected with an oil gas inlet at the lower part of the fractionating tower; an oil gas production outlet at the top of the fractionating tower is connected with an oil gas condensation cooler, and a modified asphalt production outlet at the bottom of the fractionating tower is connected with a modified asphalt delivery pipeline;
the modified asphalt production device also comprises a tubular heating furnace II, wherein a furnace tube inlet of the tubular heating furnace II is connected with a first asphalt conveying pipeline, and a furnace tube outlet is connected with a raw material asphalt conveying pipeline at the upstream of an asphalt inlet of a flash tower at the upper part of a flash modification reaction kettle; the asphalt conveying pipeline I and the asphalt conveying pipeline II are respectively provided with an asphalt circulating pump; the modified asphalt delivery pipeline is provided with a modified asphalt pump and a modified asphalt cooler; a side line flash oil circulating pipeline is arranged at the upper part of the fractionating tower, and a flash oil cooler and a circulating flash oil pump are arranged on the flash oil circulating pipeline; an oil gas outlet of the oil gas condensation cooler is connected with an oil-water separation tank, a flash oil outlet of the oil-water separation tank is connected with a flash oil circulating pipeline at the lateral line of the fractionating tower, and a non-condensable gas outlet of the oil-water separation tank is connected with a vacuum system.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710467653.4A CN107057740B (en) | 2017-06-20 | 2017-06-20 | Modified asphalt production device |
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| CN201710467653.4A CN107057740B (en) | 2017-06-20 | 2017-06-20 | Modified asphalt production device |
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| CN107057740A CN107057740A (en) | 2017-08-18 |
| CN107057740B true CN107057740B (en) | 2022-12-13 |
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| CN107400528A (en) * | 2017-09-05 | 2017-11-28 | 中冶焦耐(大连)工程技术有限公司 | A kind of modified coal tar pitch flash distillation reactor and its method of work |
| CN108315036A (en) * | 2018-02-28 | 2018-07-24 | 黄骅市信诺立兴精细化工股份有限公司 | The production technology of coalite tar heavy constituent production modified coal tar pitch in a kind of utilization |
| CN110240918B (en) * | 2019-07-19 | 2024-04-23 | 中冶焦耐(大连)工程技术有限公司 | System and process for producing modified asphalt by double-furnace double-kettle stripping flash evaporation |
| CN110240917B (en) * | 2019-07-19 | 2024-04-26 | 中冶焦耐(大连)工程技术有限公司 | System and process for producing modified asphalt by double-furnace double-kettle pressurization |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB472541A (en) * | 1936-02-24 | 1937-09-24 | Thomas Owston Wilton | Improvements in or relating to the distillation and cracking of tars, oils and like liquid hydrocarbons, and of fats |
| CA1044166A (en) * | 1975-03-06 | 1978-12-12 | Gulf Canada Limited | Petroleum pitch preparation |
| GB2087920B (en) * | 1980-11-11 | 1983-11-16 | Spencer Peter | Process and apparatus for the distillation and thermal cracking of a crude oil feedstock |
| JP4820186B2 (en) * | 2005-03-02 | 2011-11-24 | 勲 持田 | Method for producing coking binder |
| CN102311747A (en) * | 2011-08-30 | 2012-01-11 | 河南宝舜化工科技有限公司 | Furnace-kettle type modified pitch production system and production process |
| 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 |
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