CN216427210U - Modified asphalt production system - Google Patents
Modified asphalt production system Download PDFInfo
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- CN216427210U CN216427210U CN202123076485.7U CN202123076485U CN216427210U CN 216427210 U CN216427210 U CN 216427210U CN 202123076485 U CN202123076485 U CN 202123076485U CN 216427210 U CN216427210 U CN 216427210U
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Abstract
The utility model discloses a modified pitch production system can decompression low temperature polymerization, and prolong the dwell time of pitch, including first reation kettle, the second reation kettle, the flash distillation oil groove, and establish ties the modification intervalve through the pipeline in proper order between the full flow tube export of second reation kettle and the entry of cooler, modified pitch delivery pump, the modification tower, the pitch delivery route that the modification circulating pump formed, the bottom export of first reation kettle and second reation kettle communicates each other, first reation kettle, respectively establish ties a flash distillation oil cooler between the top flash distillation oil export of second reation kettle and the entry of flash distillation oil groove, the top flash distillation oil export of modification tower communicates the condensation cooler, the liquid phase export of condensation cooler communicates the flash distillation oil groove, the gaseous phase export of condensation cooler communicates the vacuum pump, the export of modification circulating pump still communicates the modification tower through the circulating pipe, first reation kettle, the top flash distillation oil cooler of modification tower is exported, A reaction kettle heating furnace is respectively arranged outside the second reaction kettle, and stirrers are respectively arranged in the first reaction kettle and the second reaction kettle.
Description
Technical Field
The utility model relates to a modified asphalt production technical field especially relates to a modified asphalt production system of low investment, energy-concerving and environment-protective effectual, product quality is stable.
Background
Nearly 55% of pitch in the coal tar processing process belongs to a bulk product of tar processing, and the larger the processing scale is, the more the pitch yield is. The modified asphalt is the main downstream product of asphalt and is mainly used for producing prebaked anodes in the electrolytic aluminum industry to prepare battery rods or electrode binders.
The modified asphalt is a product with higher added value generated in the processing of high-temperature coal tar, and is different from the high-temperature asphalt in that the high-temperature asphalt only has the requirement on the softening point, and the modified asphalt not only has the requirement on the softening point, but also has strict requirements on the content of asphalt components, coking value and the like, so that the quality of the modified asphalt can be ensured.
At present, the process for producing modified asphalt mostly adopts a thermal polycondensation method, and the thermal polycondensation method can be divided into a kettle type heating method and a tube furnace heating method according to the heating mode.
The production process of the modified asphalt by the kettle type heating method comprises the following steps: the medium temperature asphalt is used as raw material, the heating furnace directly heats the outer surface of the reaction kettle, and the reaction kettle achieves the purpose of asphalt modification by controlling certain reaction residence time and proper reaction temperature.
The production process of the modified asphalt by a tubular furnace heating method comprises the following steps: medium temperature asphalt is used as a raw material, asphalt is heated in a tubular furnace, then modification is carried out in a reaction kettle, the reaction is carried out in two steps, and the reaction time is prolonged by a stripping tower or the modification kettle after the reaction, so that the generation amounts of alpha-components and beta-components can be effectively controlled. In order to control the retention time of asphalt in a reaction kettle, the flow rate of the asphalt needs to be controlled, and the liquid level, the density and the weight of the asphalt are difficult to measure accurately, Chinese patent CN112745870A alternately arranges upper baffle plates and lower baffle plates at intervals in the reaction kettle, so that a lower asphalt flow channel is formed between the bottom of the upper baffle plate and the bottom wall of the horizontal reaction kettle, an upper asphalt flow channel is formed between the top of the lower baffle plate and the top wall of the horizontal reaction kettle, medium-temperature asphalt enters from one end of the reaction kettle, flows out from the other end, first-in first-out, last-out and then-out, and circulates for multiple times, so that all asphalt raw materials can have the same and sufficient retention time and the asphalt outflow is stable, and a liquid level regulating instrument or a weight regulating instrument is not needed.
For example, the production process of modified asphalt by a kettle type heating method disclosed in Chinese patent CN205205077U, the process flow and equipment are simple, the investment is low, the processing capacity can be controlled by increasing the number of kettles, the operation is stable, only the normal pressure polymerization production of the reaction kettles is adopted, 2-3 reaction kettles can be adopted for series production, the qualified modified asphalt enters a modified asphalt intermediate tank, the modified asphalt is cooled by a modified asphalt vaporization cooler and then is sent into an asphalt elevated tank of an asphalt forming unit, the liquid level of the last reaction kettle is controlled by an n-shaped pipe, the quality of the production system and the process modified asphalt has a single adjusting means, the temperature of the reaction kettles is high, the density is gradually reduced along with the temperature rise after the temperature rise of the asphalt, the asphalt which enters the reaction kettles is easy to sink to the bottom due to the relatively low temperature, the production period of the process depends on the capacity of the single reaction kettle and the flow rate of the asphalt raw material, and the asphalt entering the reaction kettle can not be ensured to be firstly discharged first and then discharged last, so the production period is short, and meanwhile, because the top of the n-shaped pipe can not be completely closed, the tail gas of the asphalt escapes or air enters, and the tail gas is not beneficial to the centralized collection and treatment of the tail gas for explosion prevention.
Disclosure of Invention
The utility model discloses an asphalt can be polymerization at low temperature in making the modification cauldron, and the dwell time of extension pitch in reation kettle, and collect the tail gas retrieval and utilization in the reaction, a modification pitch production system is provided, with first reation kettle, the second reation kettle is established ties and is heated the ordinary pressure polymerization, pitch after the modification flows automatically and gets into the modification middle tank, through modification pitch delivery pump to modification tower, the modification tower makes partly modification pitch carry out the cycle mixing through the modification circulating pump, partly send into the entering pitch storage tank after the vaporizer cooling, modification top of the tower is through top of the tower condensation cooler, adjust and control modification pitch quality through vacuum pump negative pressure.
The technical scheme of the utility model is that: a modified asphalt production system comprises a first reaction kettle, a second reaction kettle, a flash oil groove, and an asphalt conveying route formed by sequentially connecting a modified intermediate tank, a modified asphalt conveying pump, a modified tower and a modified circulating pump in series through pipelines between the outlet of a full flow pipe of the second reaction kettle and the inlet of a cooler, wherein the bottom outlets of the first reaction kettle and the second reaction kettle are communicated through a pipeline, a flash oil cooler is respectively connected in series between the top flash oil outlet of the first reaction kettle and the second reaction kettle and the inlet of the flash oil groove, the top flash oil outlet of the modified tower is communicated with a condensing cooler, the liquid phase outlet of the condensing cooler is communicated with the inlet of the flash oil groove, the gas phase outlet of the condensing cooler is communicated with a vacuum pump, the outlet of the modified circulating pump is also communicated with the modified tower through a circulating pipe, and a reaction kettle heating furnace is respectively arranged outside the first reaction kettle and the second reaction kettle, stirrers are arranged in the first reaction kettle and the second reaction kettle.
Preferably, a tail gas treatment device is connected in series between the outlet of the vacuum pump, the gas phase outlet of the flash oil groove and the gas phase outlet of the reforming intermediate groove and the gas phase inlet of the reaction kettle heating furnace.
Preferably, an outlet of the full flow pipe of the second reaction kettle is communicated with a liquid phase inlet at the top of the upgrading intermediate tank, the upgraded asphalt conveying pump is communicated with a liquid phase outlet at the bottom of the upgrading intermediate tank and a liquid phase inlet at the top of the upgrading tower, and an inlet and an outlet of the upgrading circulating pump are respectively communicated to the bottom and the top of the upgrading tower.
Preferably, n intermediate reaction kettles are further connected in series between the first reaction kettle and the second reaction kettle, the full flow pipe outlet of the nth intermediate reaction kettle is communicated to the bottom of the second reaction kettle, every two of the 1 st to n-1 th intermediate reaction kettles are connected in series in a mode of the nth intermediate reaction kettle and the second reaction kettle in sequence, the bottom of the 1 st intermediate reaction kettle is communicated with the bottom of the first reaction kettle, a flash evaporation oil cooler is connected in series between the top flash evaporation oil outlet of each intermediate reaction kettle and the inlet of the flash evaporation oil groove, a reaction kettle heating furnace is arranged outside each intermediate reaction kettle, and a stirrer is arranged in each intermediate reaction kettle.
The utility model has the advantages that:
1. the kettle type normal pressure self-flow production process between reaction kettles and the negative pressure production process of the modification tower are adopted, so that more pumps, flowmeters, regulating valves, tube furnaces and other equipment are saved, the investment is saved, the operation and the maintenance are convenient, and the treatment capacity and the quality are easy to adjust and control.
2. The reaction kettle heating furnace provides heat for producing modified asphalt, and simultaneously burns waste gas generated in the production process, thereby saving energy and protecting environment.
3. The reaction kettles are connected in series, the first reaction kettle and the second reaction kettle are communicated through the bottoms, and the subsequent reaction kettle automatically flows into the modification middle tank or the next reaction kettle by utilizing the principle of the communicating vessel. For example, when the low-temperature asphalt raw material is fed from the upper part of a first reaction kettle, the temperature of the asphalt raw material at the upper layer is low and the viscosity of the asphalt at the lower layer is high after the asphalt is heated, the bottom of the first reaction kettle is communicated with the bottom of a subsequent reaction kettle, the asphalt with low viscosity automatically flows to the subsequent reaction kettle due to resistance, the asphalt with high viscosity gradually falls and rises in temperature in the first reaction kettle, the temperature of the asphalt layer which firstly enters the subsequent reaction kettle is high and density is reduced, the asphalt layer floats on the asphalt layer which then enters the subsequent reaction kettle, the asphalt layer which firstly enters the subsequent reaction kettle rises to a full flow pipe and then automatically flows to the bottom of the subsequent reaction kettle, the asphalt layer at the full flow pipe at the upper part of the first reaction kettle automatically flows to the top of a modified intermediate tank, the temperature of the asphalt in the modified intermediate tank is naturally reduced because the asphalt is not heated, the temperature of the asphalt in the modified intermediate tank is greatly reduced, and the asphalt density is greatly positioned at the lower part of the asphalt which then enters the intermediate tank, the asphalt is conveyed to an upgrading tower by an upgrading asphalt conveying pump. Therefore, the asphalt is firstly input and firstly output in the production system and then output, so that all asphalt raw materials can have the same and sufficient retention time, the asphalt output is stable, and a liquid level regulating instrument or a weight regulating instrument is not needed.
4. The processing capacity can be increased by adding reaction kettles, 2, 4 or 6, and the corresponding production capacity can be selected in pairs.
5. The reforming tower adopts a negative pressure mode, and the volume of the reforming tower is large (for example, the volume is larger than 250 m)3) The additional heat is not added, the regulation elasticity of the quality of the modified asphalt can be increased, the temperature of a heating furnace of the reaction kettle is reduced to reduce the consumption of energy media, the softening point is controlled by a negative pressure value, the retention time in the modification tower is regulated by the liquid level or the feeding quantity of the modification tower, and relevant indexes such as modified asphalt toluene insoluble substances, quinoline insoluble substances, coking value and the like are regulated.
The production system has high operation flexibility, can utilize the advantage of large space of the upgrading tower, realizes the circulation of asphalt in the system when the abnormal tar distillation in the previous process cannot normally feed or start up, and avoids the stop production of the device due to material failure or slow and unqualified start-up temperature rise or more intermediate products. The specific process flow is as follows:
drawings
FIG. 1 is a schematic diagram of an upgraded asphalt production system;
FIG. 2 is a schematic diagram of another embodiment of an upgraded asphalt production system;
wherein: the system comprises a first reaction kettle 1, a first reaction kettle heating furnace 2, a first reaction kettle stirrer 3, a second reaction kettle 4, a second reaction kettle heating furnace 5, a second reaction kettle stirrer 6, a first flash oil cooler 7, a second flash oil cooler 8, a flash oil groove 9, a modified middle tank 10, a modified asphalt conveying pump 11, a modified tower top condensation cooler 12, a modified tower 13, a vacuum pump 14, a modified circulating pump 15, a full flow pipe 16, a circulating pipe 17, a 1 st middle reaction kettle 18 and a 2 nd middle reaction kettle 19.
Detailed Description
The present invention is described in further detail below with reference to the following figures and specific examples, which should not be construed as limiting the invention.
Example 1
Referring to fig. 1, a modified asphalt production system comprises a first reaction vessel 1, a second reaction vessel 4, a flash oil tank 9, and an asphalt conveying line formed by sequentially connecting a modified intermediate tank 10, a modified asphalt conveying pump 11, a modifying tower 13 and a modified circulating pump 15 in series between the outlet of a full flow pipe 16 of the second reaction vessel 4 and the inlet of a cooler through pipelines, wherein the bottom outlets of the first reaction vessel 1 and the second reaction vessel 2 are communicated through a pipeline, a flash evaporator 7/8 is respectively connected in series between the top flash oil outlets of the first reaction vessel 1 and the second reaction vessel 4 and the top liquid inlet of the flash oil tank 9, the top flash oil outlet of the modifying tower 13 is communicated with a condensing cooler 12, the liquid outlet of the condensing cooler 12 is communicated with the top liquid inlet of the flash oil tank 9, the gas outlet of the condensing cooler 12 is communicated with a vacuum pump 14, the outlet of the modified circulating pump 15 is also communicated to the top of the modifying tower 13 through a circulating pipe 17, a reaction kettle heating furnace 2/5 is respectively arranged outside the first reaction kettle 1 and the second reaction kettle 4, and stirrers 3/6 are respectively arranged in the first reaction kettle 1 and the second reaction kettle 4. A tail gas treatment device is connected in series between the outlet of the vacuum pump 14, the gas phase outlets of the flash oil groove 9 and the reforming intermediate groove 10 and the gas phase inlet of the reaction kettle heating furnace 2/5. An outlet of a full flow pipe 16 of the second reaction kettle 6 is communicated with a liquid phase inlet at the top of the upgrading intermediate tank 10, an upgrading asphalt conveying pump 11 is communicated with a liquid phase outlet at the bottom of the upgrading intermediate tank 10 and a liquid phase inlet at the top of the upgrading tower 13, and an inlet and an outlet of the upgrading circulating pump 11 are respectively communicated with the bottom and the top of the upgrading tower 13.
The process for producing the modified asphalt by the system comprises the following steps:
asphalt from a tar distillation device in an upstream process directly enters a first reaction kettle 1 through a pipeline, the first reaction kettle 1 is connected to a second reaction kettle 4 through a bottom communicating pipe, a full flow pipe at the top of the second reaction kettle 4 directly and fully flows to a modified intermediate tank 10, the first reaction kettle 1 is heated through a first reaction kettle heating furnace 2, the second reaction kettle 4 is heated through a second reaction kettle heating furnace 5, flash oil at the top of the first reaction kettle 1 is cooled through a first flash oil cooler 7 and then enters a flash oil tank 9, a second flash oil cooler 8 at the top of the second reaction kettle 4 is cooled and then enters a flash oil tank 9, modified asphalt in the modified intermediate tank 10 enters a modified tower 13 through a modified asphalt conveying pump 11, flash oil at the top of the modified tower 13 enters a condensation cooler 12 at the top of the modified tower, is pumped out through a vacuum pump 14 and then is treated through a tail gas treatment device and then enters the first reaction kettle heating furnace 2 for incineration, the tail gas of the flash oil tank 9 and the modified intermediate tank 10 is treated by a tail gas treatment device and then sent to a second reaction kettle heating furnace 5 for incineration, part of the asphalt in the modified tower 13 is circulated in the tower through a modified circulating pump 15, and part of the asphalt is cooled by a cooler and then sent to the next process.
As shown in FIG. 2, on the basis of the device in FIG. 1, the processing capacity can be increased by adding reaction kettles, 2, 4 or 6, and the corresponding production capacity can be selected in a group of two. The specific improvement measures are as follows: still connect 2 intermediate reaction cauldron 18/19 in series between first reation kettle 1 and the second reation kettle 4, 2 nd intermediate reaction cauldron 19's full flow pipe export communicates to the bottom of second reation kettle 4, the bottom of 1 st intermediate reaction cauldron 18 and first reation kettle 1's bottom intercommunication, 1 st intermediate reaction cauldron 18's full flow pipe export communicates to the bottom of 2 nd intermediate reaction cauldron 19, a flash oil cooler of respectively establishing ties between two intermediate reaction cauldron's top flash distillation oil export and flash oil groove 9's the entry, two intermediate reaction cauldron all set up a reation kettle heating furnace outward, all be equipped with the agitator in two intermediate reaction kettles.
Claims (4)
1. A modified asphalt production system is characterized by comprising a first reaction kettle, a second reaction kettle, a flash oil tank and an asphalt conveying route formed by sequentially connecting a modified intermediate tank, a modified asphalt conveying pump, a modifying tower and a modified circulating pump in series through pipelines between an outlet of a full flow pipe of the second reaction kettle and an inlet of a cooler, wherein outlets at the bottoms of the first reaction kettle and the second reaction kettle are communicated through pipelines, a flash evaporator is respectively connected in series between an outlet of flash oil at the top of the first reaction kettle and the second reaction kettle and an inlet of the flash oil tank, an outlet of flash oil at the top of the modifying tower is communicated with a condensing cooler, a liquid phase outlet of the condensing cooler is communicated with an inlet of the flash oil tank, a gas phase outlet of the condensing cooler is communicated with a vacuum pump, an outlet of the modified circulating pump is also communicated with the modifying tower through a circulating pipe, and an oil cooler of the first reaction kettle is communicated with the modifying tower through a circulating pipe, A reaction kettle heating furnace is respectively arranged outside the second reaction kettle, and stirrers are respectively arranged in the first reaction kettle and the second reaction kettle.
2. The modified asphalt production system according to claim 1, wherein a tail gas treatment device is connected in series between the outlet of the vacuum pump, the gas phase outlets of the flash oil tank and the modified intermediate tank, and the gas phase inlet of the reaction kettle heating furnace.
3. The modified asphalt production system of claim 2, wherein the full flow pipe outlet of the second reaction kettle is communicated with the liquid phase inlet at the top of the modified intermediate tank, the modified asphalt conveying pump is communicated with the liquid phase outlet at the bottom of the modified intermediate tank and the liquid phase inlet at the top of the modified tower, and the inlet and the outlet of the modified circulating pump are respectively communicated with the bottom and the top of the modified tower.
4. The modified asphalt production system of claim 3, wherein n intermediate reaction kettles are further connected in series between the first reaction kettle and the second reaction kettle, the full flow pipe outlet of the nth intermediate reaction kettle is communicated to the bottom of the second reaction kettle, 1-n-1 intermediate reaction kettles are sequentially connected in series in such a way that every two intermediate reaction kettles form one group according to the nth intermediate reaction kettle and the second reaction kettle, the bottom of the 1 st intermediate reaction kettle is communicated with the bottom of the first reaction kettle, a flash evaporator is respectively connected in series between the top flash oil outlet of each intermediate reaction kettle and the inlet of the flash oil tank, a reaction kettle heating furnace is arranged outside each intermediate reaction kettle, and an oil cooler is arranged in each intermediate reaction kettle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123076485.7U CN216427210U (en) | 2021-12-09 | 2021-12-09 | Modified asphalt production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123076485.7U CN216427210U (en) | 2021-12-09 | 2021-12-09 | Modified asphalt production system |
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| CN216427210U true CN216427210U (en) | 2022-05-03 |
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| CN202123076485.7U Active CN216427210U (en) | 2021-12-09 | 2021-12-09 | Modified asphalt production system |
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2021
- 2021-12-09 CN CN202123076485.7U patent/CN216427210U/en active Active
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