CN107057740B - Modified asphalt production device - Google Patents

Abstract

The invention relates to a modified asphalt production device. The asphalt inlet of the flash tower on the upper part of the flash reforming reactor is connected to a raw material asphalt conveying pipeline, and the oil and gas extraction outlet of the flash tower is connected to an oil and gas condensation cooler; the asphalt outlet of the lower reaction kettle is connected to The furnace tube inlet of tubular heating furnace 1 and the furnace tube outlet of tubular heating furnace 1 are connected to the asphalt inlet of the secondary reforming reactor; the bitumen outlet of the secondary reforming reactor is connected to the asphalt conveying upstream of tubular heating furnace 1 Pipeline one and the other are connected to the asphalt inlet of the fractionation tower; the oil and gas outlet of the secondary reforming reactor is connected to the oil and gas inlet at the lower part of the fractionation tower; the oil and gas outlet of the fractionation tower is connected to the oil and gas condensation cooler, and the modified asphalt outlet of the fractionation tower Connect the modified asphalt delivery pipeline. The invention adopts a two-step reaction method in two kettles, which can effectively control the production amount of α-component and β-component, and the product quality is controllable; the process is simple and easy, energy-saving and environment-friendly, and is applicable to various asphalt raw materials.

Description

A modified asphalt production device

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 technique

Coal tar processing generally produces about 50% to 60% of asphalt, which is a bulk product of tar processing. The larger the processing scale, the more asphalt output. Modified asphalt is currently the main downstream product of asphalt, which is mainly used in the electrolytic aluminum industry to produce prebaked anodes, and to prepare battery rods or electrode binders.

At present, domestic production of modified asphalt mostly adopts kettle-type thermal condensation polymerization process. This process uses medium-temperature asphalt as raw material, and achieves the purpose of asphalt modification by controlling a certain reaction residence time and appropriate reaction temperature in a reactor directly heated by a heating furnace. Since the heating surface is the outer surface of the reactor, in order to achieve a good mass and heat transfer effect, the reactor needs to be equipped with a stirrer, so that the volume of the reactor is limited. Therefore, in order to achieve a suitable reaction time, generally two to three Kettles operate in series. In addition, due to the sealing problem of the agitator at high temperature, the modification reaction generally adopts normal pressure reaction. The process flow of the kettle-type thermal polycondensation process is short, and the process is simple and easy; its disadvantages are that the equipment and pipelines are easy to coke, the reaction controllability is poor, the operation is very inconvenient, the heating in the reactor is uneven, the product quality is poor, and it is limited by the volume of the kettle , the design capacity of each series is limited.

In order to improve the shortcomings of the above-mentioned processes, there have been modified asphalt processes heated by tubular furnaces, such as the pressurized double-furnace double-kettle stripping flash process imported from France, and the domestic single-furnace single-kettle stripping flash process.

The pressurized double kettle double furnace stripping and flashing process uses medium temperature asphalt as raw material, heats the asphalt in the tubular heating furnace, and then reacts in the reaction kettle. The reaction is carried out in two steps, and it is a pressurized reaction. After the reaction, it is flash stripped in a stripping tower. The advantage of this process is that it adopts two-step reaction, which can effectively control the amount of α-component and β-component, and the product quality is controllable; the pressurized reaction is conducive to the formation of β-resin and improves the coking value; the asphalt is separated by steam stripping And oil products, it is beneficial to adjust the softening point; the disadvantage is that the asphalt is easy to coke during the pressurized reforming reaction, and the energy consumption is also high; the separation of asphalt and oil products by steam stripping will also generate a large amount of process wastewater.

The single-furnace single-pot stripping flash process also uses medium-temperature asphalt as raw material. The asphalt is heated in a tubular heating furnace, and then reacted in a reactor. The reaction is completed in one step, which is a pressurized reaction. After the reaction, it is flash stripped in the stripping column. The advantage of this process is one-step reaction, short process flow, relatively low energy consumption, pressurized reaction is conducive to the formation of β-resin, and improves the coking value. The disadvantage is that the one-step reaction requires high temperature and time control, and the product quality is difficult to control; the separation of asphalt and oil products by steam stripping will also produce a large amount of process wastewater.

To sum up, there is currently no relatively complete modified asphalt production device in China that is suitable for various asphalt raw materials, energy-saving and environmentally friendly, and has excellent product quality.

Contents of the invention

The invention provides a modified asphalt production device, which adopts a two-pot two-step reaction method, can effectively control the production of α-component and β-component, and controllable product quality; the process is simple, energy-saving and environmentally friendly, and is suitable for For various asphalt raw materials.

In order to achieve the above object, the present invention adopts the following technical solutions to realize:

A modified asphalt production device, including a flash reforming reactor, a tubular heating furnace, a secondary reforming reactor and a fractionation tower; the flash reforming reactor is composed of an upper flash tower and a The lower part of the reaction kettle is composed of the asphalt inlet of the flash tower connected to the raw asphalt conveying pipeline, the oil and gas extraction outlet at the top of the flash tower is connected to the oil and gas condensation cooler; the asphalt outlet at the bottom of the reaction kettle is connected to the furnace tube inlet of the tubular heating furnace 1, The outlet of the furnace tube of the type heating furnace 1 is connected to the asphalt inlet on the upper part of the secondary reforming reactor; the asphalt outlet at the bottom of the secondary reforming reactor is divided into two routes, one is connected to the asphalt inlet in the middle of the fractionating tower through the second asphalt conveying pipeline, and the other is One road is connected to the asphalt conveying pipeline 1 upstream of the inlet of the tube heating furnace 1; the oil and gas extraction outlet on the top of the secondary reforming reactor is connected to the oil and gas inlet at the lower part of the fractionation tower; the oil and gas extraction outlet on the top of the fractionation tower is connected to the oil and gas condensation cooler, The modified asphalt outlet at the bottom of the tower is connected to the modified asphalt delivery pipeline.

It also includes the second tubular heating furnace, the inlet of the furnace tube of the second tube heating furnace is connected to the asphalt conveying pipeline one, and the outlet of the furnace tube is connected to the raw asphalt conveying pipeline upstream of the asphalt inlet of the flash tower at the upper part of the flash reforming reactor.

Bitumen circulation pumps are respectively arranged on the first bitumen delivery pipeline and the second bitumen delivery pipeline.

A modified asphalt pump and a modified asphalt cooler are arranged on the modified asphalt delivery pipeline.

A side line flash oil circulation pipeline is arranged on the upper part of the fractionation tower, and a flash oil cooler and a circulating flash oil pump are arranged on the flash oil circulation pipeline.

The oil and gas outlet of the oil-gas condensing cooler is connected to the oil-water separation tank, the flash oil outlet of the oil-water separation tank is connected to the flash oil circulation pipeline of the side line of the fractionation tower, and the non-condensable gas outlet of the oil-water separation tank is connected to the vacuum system.

Compared with prior art, the beneficial effect of the present invention is:

1) The technological process is short and simple;

2) The negative pressure reforming operation is used to reduce the reaction temperature, which can effectively reduce the possibility of coking of equipment and pipelines;

3) By controlling the reaction time and temperature, the β-resin content and coking value of the asphalt product can be effectively increased, so that the product quality of the modified asphalt can be controlled;

4) The two-step reaction in double tanks is adopted, and the β-modification and α-modification are carried out in two reactors respectively, which ensures the control flexibility of the modification reaction and can meet the diversified requirements of product quality;

5) The flash function is added before the first polycondensation reaction, which can meet the requirements of diversification of raw materials;

6) The process of separating oil and asphalt by fractionating tower can not only improve the separation efficiency; but also avoid a large amount of process wastewater, which is energy-saving and environmentally friendly;

7) Through the reasonable layout and design of the tube furnace, the process of single furnace and double kettle can be realized.

Description of drawings

Fig. 1 is a structural schematic diagram of a modified asphalt production device according to the present invention.

In the figure: 1. Flash reforming reactor 2. Secondary reforming reactor 31. Tubular heating furnace 1 32. Tubular heating furnace 2 4. Asphalt circulation pump 5. Fractionation tower 6. Modified asphalt pump 7. Modified asphalt cooler 8. Oil-gas condensation cooler 9. Oil-water separation tank 10. Circulating flash oil pump 11. Flash oil cooler

A. Raw asphalt B. Modified asphalt C. Non-condensable gas D. Flash oil

detailed description

The specific embodiment of the present invention will be further described below in conjunction with accompanying drawing:

As shown in Figure 1, a modified asphalt production device according to the present invention includes a flash reforming reactor 1, a tubular heating furnace 31, a secondary reforming reactor 2 and a fractionation tower 5; The upgrading reaction kettle 1 is composed of a connected upper flash tower and a lower reaction kettle. The asphalt inlet of the flash tower is connected to the raw asphalt conveying pipeline, and the oil and gas extraction outlet at the top of the flash tower is connected to the oil and gas condensation cooler 8; The asphalt outlet at the bottom is connected to the furnace tube inlet of tubular heating furnace 1 31, and the furnace tube outlet of tubular heating furnace 1 31 is connected to the asphalt inlet on the upper part of the secondary reforming reactor 2; the bottom asphalt outlet of the secondary reforming reactor 2 Divided into two roads, one road is connected to the asphalt inlet in the middle part of the fractionation tower 5 through the asphalt conveying pipeline 2, and the other road is connected to the asphalt conveying pipeline 1 upstream of the tubular heating furnace 1 31 furnace tube entrance; The outlet is connected to the oil and gas inlet at the lower part of the fractionation tower 5; the oil and gas extraction outlet at the top of the fractionation tower 5 is connected to the oil and gas condensation cooler 8, and the modified asphalt extraction outlet at the bottom of the fractionation tower 5 is connected to a modified asphalt delivery pipeline.

It also includes a tube heating furnace 2 32, the furnace tube inlet of the tube heating furnace 2 32 is connected to the bitumen delivery pipeline 1, and the furnace tube outlet is connected to the raw material bitumen delivery pipeline upstream of the flash tower bitumen inlet on the upper part of the flash reforming reactor 1.

Bitumen circulation pumps 4 are respectively arranged on the first bitumen delivery pipeline and the second bitumen delivery pipeline.

The modified asphalt delivery pipeline is provided with a modified asphalt pump 6 and a modified asphalt cooler 7 .

The upper part of the fractionation tower 5 is provided with a side line flash oil circulation pipeline, and a flash oil cooler 11 and a circulating flash oil pump 10 are provided on the flash oil circulation pipeline.

The oil and gas outlet of the oil-gas condensing cooler 8 is connected to the oil-water separation tank 9, the flash oil outlet of the oil-water separation tank 9 is connected to the flash oil circulation pipeline of the side line of the fractionation tower 5, and the non-condensable gas outlet of the oil-water separation tank 9 is connected to the vacuum system .

The raw material asphalt A is first mixed with the outlet asphalt of the tubular heating furnace 2 32, and then enters the flash tower at the top of the flash reforming reactor 1 together, and the flashed asphalt falls into the reactor at the lower part of the flash reforming reactor 1 The modification reaction takes place inside; during the modification reaction, the temperature in the reactor is controlled at 330-400°C, and the asphalt mainly undergoes β-modification reaction;

The light oil product flashed out in the upper flash tower and the reaction gas cracked in the lower reactor conduct mass transfer and heat transfer in the flash tower, and the heavy oil falls into the reactor to continue the reforming reaction. The oil product leaves from the top of the flash tower and enters the oil-gas condensing cooler 8, and the cooled light oil product is collected as flash oil D, and the non-condensable gas C enters the vacuum system to ensure that the reforming reaction is carried out under negative pressure;

Most of the asphalt sent from the bottom of the flash reforming reaction kettle 1 enters the tubular heating furnace 2 32 for circulation heating, and the other small part is first mixed with the asphalt at the bottom of the secondary reforming reaction kettle, then enters the tubular heating furnace 1 31 for heating, and then enters the Secondary modification reaction kettle 2; the temperature inside the second modification reaction kettle 2 is controlled at 350-420°C, and the asphalt mainly undergoes α-modification reaction; most of the asphalt at the bottom of the second modification reaction kettle 2 is sent to the tubular Heating furnace one 31 circulates heating, and a small part is sent to the fractionation tower 5; the cracked gas at the top of the secondary reforming reaction tank also enters the fractionation tower 5;

The bitumen after twice upgrading realizes the separation of bitumen and oil products in the fractionating tower 5; the light oil products leave from the top of the tower and enter the oil-gas condensation cooler 8, and the cooled light oil products are collected as flash oil D, The non-condensable gas C enters the vacuum system to ensure that the reforming reaction in the secondary reforming reactor 2 and the fractionation process in the fractionating tower 5 are also carried out under negative pressure; the flash oil D extracted from the side line of the fractionating tower 5 is cooled Finally, part of it is sent out as flash oil product, and the rest is sent to the top of the fractionating tower as reflux, and the modified bitumen B is extracted from the bottom of the fractionating tower.

The above is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto, any person familiar with the technical field within the technical scope disclosed in the present invention, according to the technical solution of the present invention Any equivalent replacement or change of the inventive concepts thereof shall fall within the protection 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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