CN210560259U - System for producing modified asphalt by double-furnace double-kettle stripping flash evaporation - Google Patents
System for producing modified asphalt by double-furnace double-kettle stripping flash evaporation Download PDFInfo
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- CN210560259U CN210560259U CN201921145449.1U CN201921145449U CN210560259U CN 210560259 U CN210560259 U CN 210560259U CN 201921145449 U CN201921145449 U CN 201921145449U CN 210560259 U CN210560259 U CN 210560259U
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- 238000001704 evaporation Methods 0.000 title claims abstract description 28
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 113
- 238000005303 weighing Methods 0.000 claims description 26
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- 238000004519 manufacturing process Methods 0.000 abstract description 10
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- 238000005259 measurement Methods 0.000 description 12
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- 239000000203 mixture Substances 0.000 description 7
- 238000007599 discharging Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 5
- 238000007701 flash-distillation Methods 0.000 description 4
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- 238000006068 polycondensation reaction Methods 0.000 description 2
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- 239000010959 steel Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
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- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
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Abstract
The utility model relates to a system for producing modified asphalt by double-furnace double-kettle stripping flash evaporation, which comprises a 1# reaction kettle, a 1# full-flow buffer tank, a 1# tubular furnace, a first asphalt circulation loop, a 2# reaction kettle, a 2# full-flow buffer tank, a 2# tubular furnace and a second asphalt circulation loop; flexible baffles are respectively arranged in the No. 1 reaction kettle and the No. 2 reaction kettle, and a No. 1 full flow buffer tank is arranged on the first asphalt circulating loop; and a No. 2 full flow buffer tank is arranged on the second asphalt circulating loop. The utility model discloses in, reation kettle changes the side feeding into by side feeding, lower ejection of compact mode, full flow ejection of compact mode, establishes the full flow buffer tank behind reation kettle, through the pitch liquid level that maintains in the full flow buffer tank stable outflow that controls reation kettle, finally realizes the accurate control of reaction dwell time through the liquid level invariant in the control reation kettle to make modified asphalt production process carry out for a long time and smoothly.
Description
Technical Field
The utility model relates to a metallurgical coking technical field especially relates to a system for two stoves strip flash distillation production modified pitch of two kettles.
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, preparing battery rods or electrode binders in the electrolytic aluminum industry.
At present, the domestic technology 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 modified asphalt by tank-type heating method uses medium-temp asphalt as raw material, and uses a heating furnace to directly heat the external surface of reaction kettle, and the interior of reaction kettle can be controlled by means of controlling a certain reaction residence time and proper reaction temp. so as to attain the goal of modifying asphalt. 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 the design capability is limited.
A process for preparing modified asphalt by tubular furnace heating method includes such steps as pressurizing dual-furnace dual-kettle stripping flash evaporation process introduced from France, ordinary-pressure or reduced-pressure dual-furnace stripping flash evaporation process and single-furnace single-kettle stripping flash evaporation process, in which the intermediate-temp asphalt is used as raw material, the asphalt is heated in tubular heating furnace, and the modification reaction is performed in reactor.
The production process of modified asphalt by a tubular furnace heating method has become the mainstream of the existing modified asphalt production process due to large design capability and flexible reaction control, but has a great problem which is difficult to solve, namely the problem of liquid level measurement of a modified asphalt reaction kettle.
The traditional reaction kettle liquid level remote transmission measurement method generally adopts a pressure difference measurement mode, liquid density calculation is converted into liquid level height, but due to the particularity of asphalt liquid, the temperature in a reaction kettle is higher than 380 ℃, the liquid contains solid suspended matters such as polymers and the like, the liquid has high viscosity and is easy to solidify, the asphalt smoke has high volatilization and is easy to condense, and the like, at an instrument liquid pressure measurement interface, asphalt is easy to solidify and block, so that a measurement instrument fails. If a buoy liquid level meter is adopted, the buoy and the guide cylinder or the guide steel wire are easily adhered together and are not easy to float up and down, so that the liquid level measurement cannot be realized. In addition, a floating ball liquid level meter is adopted in an attempt, but the liquid level of the reaction kettle is higher than 10m, and the traditional floating ball liquid level meter is provided with a liquid level indicator with the same height as the liquid level, so that the lifting rod of the floating ball liquid level meter is too long, the liquid level indicator is too high at the top of the reaction kettle and is difficult to realize, and the floating ball and the guide cylinder or the guide steel wire are easily adhered together and are difficult to float up and down. In addition, asphalt smoke is easy to enter the liquid level indicator along the lifting rod of the liquid level indicator to generate condensation, so that the liquid level indicator is blocked. If adopt radar level gauge, the short time measurement effect still can, but because the easy condensation that produces of pitch cigarette on radar level gauge, just can make radar electromagnetic wave receive failure soon, lead to overhauing frequently.
In the pressure double-furnace double-kettle stripping flash evaporation process introduced in France, the liquid level height control of a reaction kettle does not adopt a liquid level measurement method, but adopts a weighing module to convert the liquid level height, the liquid level height is controlled by controlling the whole weight of the reaction kettle, the number of measurement points of the weighing module is the key for measuring the weight accuracy or not, generally 2 measurement points are more accurate, the number of support lugs of a large-scale reaction kettle is generally 6 or 8, the measurement is inaccurate, the influence of wind load and weighing module errors is often caused, the weight measurement is unstable, the fluctuation is large, the liquid level calculated is unstable, the fluctuation of the outflow of modified asphalt is large, and the quality control of the modified asphalt is influenced. Meanwhile, the reaction kettle has huge appearance, so that the weighing module is very difficult to overhaul and replace, the overhaul time is long, and the normal production is seriously influenced.
In conclusion, in the conventional production process of modified asphalt by a tubular furnace heating method, the problem of liquid level measurement of a reaction kettle is not well solved, so that the automation control of the process is to be perfected, and the process and equipment are to be improved.
Disclosure of Invention
The utility model provides a system for two stoves double reactor strip flash distillation production upgrading pitch, reation kettle is by the side feeding, the bottom discharge mode changes the side feeding, full flow discharge mode, establishes the full flow buffer tank behind reation kettle, and the outflow through keeping the pitch liquid level in the full flow buffer tank stable controls reation kettle, finally realizes the accurate control of reaction dwell time through the liquid level invariant in the control reation kettle to make upgrading pitch production process carry out for a long time and smoothly.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a system for producing modified asphalt by double-furnace double-kettle stripping flash evaporation comprises a No. 1 reaction kettle, a No. 1 full-flow buffer tank, a No. 1 tubular furnace, a first asphalt circulation loop, a No. 2 reaction kettle, a No. 2 full-flow buffer tank, a No. 2 tubular furnace and a second asphalt circulation loop; the middle parts of the 1# reaction kettle and the 2# reaction kettle are respectively provided with a flexible baffle with a snake-shaped cross section, the 1# reaction kettle/the 2# reaction kettle is divided into 2 independent reaction areas, and the 2 reaction areas are communicated through an asphalt flow channel below the flexible baffle; an asphalt feeding hole is formed in the upper portion of the No. 1 reaction kettle/No. 2 reaction kettle on one side of the flexible baffle, and an asphalt full-flow port is formed in the upper portion of the No. 1 reaction kettle/No. 2 reaction kettle on the other side of the flexible baffle; a first asphalt circulation loop is arranged between an asphalt full-flow port and an asphalt feed port of the No. 1 reaction kettle, and a No. 1 full-flow buffer tank, a No. 1 asphalt circulation pump, an asphalt outflow port I, an asphalt inflow port I and a No. 1 tubular furnace are sequentially arranged on the first asphalt circulation loop along the asphalt conveying direction; wherein the asphalt inflow port I is connected with an external raw asphalt conveying pipeline; a second asphalt circulation loop is arranged between an asphalt full-flow port and an asphalt feeding port of the No. 2 reaction kettle, and a No. 2 full-flow buffer tank, a No. 2 asphalt circulation pump, an asphalt inflow port II, an asphalt outflow port II and a No. 2 tubular furnace are sequentially arranged on the second asphalt circulation loop along the asphalt conveying direction; the first asphalt outflow port on the first asphalt circulation loop is connected with the second asphalt inflow port on the second asphalt circulation loop through the first asphalt conveying pipeline, and the second asphalt outflow port on the second asphalt circulation loop is connected with the asphalt inlet of the stripping tower through the second asphalt conveying pipeline; the flash evaporation oil gas outlet at the top of the No. 1 reaction kettle and the flash evaporation oil gas outlet at the top of the No. 2 reaction kettle are connected with the oil gas inlet of the stripping tower through flash evaporation oil gas conveying pipelines.
The No. 1 reaction kettle is provided with a plurality of asphalt full-flow ports along the height direction, each asphalt full-flow port is connected with a first asphalt circulation loop through a full-flow pipe I, and the full-flow pipe I is provided with a full-flow valve I; and the No. 2 reaction kettle is provided with a plurality of asphalt full-flow ports along the height direction, each asphalt full-flow port is respectively connected with a second asphalt circulation loop through a full-flow pipe II, and the full-flow pipes II are respectively provided with a full-flow valve II.
A first flow regulating valve is arranged at the upstream of the first asphalt conveying pipeline, a 1# full-flow buffer tank is supported on a 1# weighing module through 2 support lugs, and the 1# weighing module is connected with the first flow regulating valve through a weight display controller; and a second flow regulating valve is arranged at the upstream of the second asphalt conveying pipeline, the 2# full-flow buffer tank is supported on the 2# weighing module through 2 support lugs, and the 2# weighing module is connected with the second flow regulating valve through a second weight display controller.
Compared with the prior art, the beneficial effects of the utility model are that:
1)2 reaction kettles are changed from a side feeding mode and a bottom discharging mode into a side feeding mode and a full-flow discharging mode, so that the liquid level control is easy, and the reaction residence time of the asphalt in the reaction kettles can be accurately controlled;
2) the reaction kettle is not provided with a liquid level meter or a weighing module, so that the investment is reduced, the problems of frequent and difficult maintenance of a liquid level control device are solved, and the double-furnace double-kettle steam stripping flash evaporation process can stably run for a long time;
3) in order to keep the modified asphalt outflow of the reaction kettle stable, a full-flow buffer tank is arranged on the asphalt discharge pipeline, and the asphalt outflow of the reaction kettle is controlled by controlling the liquid level stability of the full-flow buffer tank; the full-flow buffer tank adopts a vertical small storage tank form with 2 support lugs, and the liquid level is measured by the weighing module, so that the accuracy and the stability of measurement can be ensured; the capacity of full flow buffer tank is little, compares with the weighing module of setting on reation kettle, and it is more convenient to change and overhaul.
Drawings
FIG. 1 is a schematic structural diagram of a system for producing modified asphalt by double-furnace double-kettle stripping flash distillation.
3 FIG. 3 2 3 is 3 a 3 sectional 3 view 3 A 3- 3 A 3 / 3 B 3- 3 B 3 in 3 FIG. 3 1 3. 3
In the figure: 1.1# reaction kettle 2.1# full flow buffer tank 3.1# asphalt circulating pump 4.1# tube furnace 5, flexible baffle 6, support lug 7.1# weighing module 8, flow regulating valve I9, full flow valve I10.2 # reaction kettle 11.2# full flow buffer tank 12.2# asphalt circulating pump 13.2# tube furnace 14.2# weighing module 15, flow regulating valve II 16, full flow valve II WRC01, weight display controller I WRC02, weight display controller II
Detailed Description
The following description of the embodiments of the present invention will be made with reference to the accompanying drawings:
as shown in fig. 1, the system for producing modified asphalt by double-furnace double-kettle stripping flash evaporation of the present invention comprises a 1# reaction kettle 1, a 1# full-flow buffer tank 2, a 1# tubular furnace 4, a first asphalt circulation loop, a 2# reaction kettle 10, a 2# full-flow buffer tank 11, a 2# tubular furnace 13 and a second asphalt circulation loop; the middle parts of the 1# reaction kettle 1 and the 2# reaction kettle 10 are respectively provided with a flexible baffle 5 (shown in figure 2) with a snake-shaped cross section, the 1# reaction kettle 1/2# reaction kettle 10 is divided into 2 independent reaction areas, and the 2 reaction areas are communicated through an asphalt flow channel below the flexible baffle 5; an asphalt feeding hole is formed in the upper portion of the No. 1/2 reaction kettle 10 of the No. 1 reaction kettle on one side of the flexible baffle 5, and an asphalt full flow port is formed in the upper portion of the No. 1/2 reaction kettle 10 of the No. 1 reaction kettle on the other side of the flexible baffle 5; a first asphalt circulation loop is arranged between an asphalt full-flow port and an asphalt feeding port of the No. 1 reaction kettle 1, and a No. 1 full-flow buffer tank 2, a No. 1 asphalt circulation pump 3, an asphalt outflow port I, an asphalt inflow port I and a No. 1 tubular furnace 4 are sequentially arranged on the first asphalt circulation loop along the asphalt conveying direction; wherein the asphalt inflow port I is connected with an external raw asphalt conveying pipeline; a second asphalt circulation loop is arranged between an asphalt full-flow port and an asphalt feeding port of the No. 2 reaction kettle 10, and a No. 2 full-flow buffer tank 11, a No. 2 asphalt circulation pump 12, an asphalt inflow port II, an asphalt outflow port II and a No. 2 tubular furnace 13 are sequentially arranged on the second asphalt circulation loop along the asphalt conveying direction; the first asphalt outflow port on the first asphalt circulation loop is connected with the second asphalt inflow port on the second asphalt circulation loop through the first asphalt conveying pipeline, and the second asphalt outflow port on the second asphalt circulation loop is connected with the asphalt inlet of the stripping tower through the second asphalt conveying pipeline; the flash evaporation oil gas outlet at the top of the No. 1 reaction kettle and the flash evaporation oil gas outlet at the top of the No. 2 reaction kettle 10 are connected with the oil gas inlet of the stripping tower through flash evaporation oil gas conveying pipelines.
The No. 1 reaction kettle 1 is provided with a plurality of asphalt full flow ports along the height direction, each asphalt full flow port is connected with a first asphalt circulation loop through a full flow pipe I, and the full flow pipe I is provided with a full flow valve I9; and the No. 2 reaction kettle 10 is provided with a plurality of asphalt full flow ports along the height direction, each asphalt full flow port is respectively connected with a second asphalt circulation loop through a full flow pipe II, and the full flow pipe II is respectively provided with a full flow valve II 16.
A first flow control valve 8 is arranged at the upstream of the first asphalt conveying pipeline, the 1# full-flow buffer tank 2 is supported on a 1# weighing module 7 through 2 support lugs 6, and the 1# weighing module 7 is connected with the first flow control valve 8 through a first weight display controller WRC 01; and a second flow regulating valve 15 is arranged at the upstream of the second asphalt conveying pipeline, the 2# full-flow buffer tank 11 is supported on the 2# weighing module 14 through the 2 support lugs 6, and the 2# weighing module 14 is connected with the second flow regulating valve 15 through a second weight display controller WRC02.
The technical process of the system for producing modified asphalt by double-furnace double-kettle stripping flash distillation is as follows:
1) the method comprises the following steps of mixing raw material medium-temperature asphalt with asphalt at an outlet of a No. 1 tubular furnace, then feeding the mixture into a reaction area at one side of a No. 1 reaction kettle 1 corresponding to an asphalt feeding port, enabling the mixture to flow from top to bottom, then feeding the mixture into a reaction area at one side of an asphalt full flow port through an asphalt flow channel below a flexible baffle 5, enabling the mixture to flow from bottom to top, controlling the reaction temperature in the No. 1 reaction kettle 1 to be 350-410 ℃, enabling the mixed asphalt to perform primary modification reaction mainly comprising β -modification reaction in the No. 1 reaction kettle 1, discharging flash evaporation oil gas generated by flash evaporation cracking to a stripping tower through a flash evaporation oil gas outlet at the top of the No. 1 reaction kettle 1, and enabling the asphalt after the primary modification reaction to fully flow into a No. 1;
2) the primary modified asphalt in the No. 1 full flow buffer tank 2 is pumped out from the bottom by a No. 1 asphalt circulating pump 3, most of the primary modified asphalt is sent into a No. 1 tubular furnace 4, and the heated primary modified asphalt is circulated and sent back to a raw material asphalt conveying pipeline at the upstream of an asphalt feeding hole of a No. 1 reaction kettle 1 to heat the raw material medium-temperature asphalt; the remaining primary modified asphalt is sent to a second asphalt circulating pipeline;
3) mixing a part of the primary modified asphalt in the second asphalt circulating pipeline with secondary modified asphalt pumped from a 2# full-flow buffer tank 11, feeding the mixture into a 2# tubular furnace 13, heating the mixture, feeding the mixture into a 2# reaction kettle 10 to perform secondary modification reaction, wherein the secondary modification reaction process is the same as the primary modification reaction process, the reaction temperature in the 2# reaction kettle 10 is controlled to be 370-430 ℃, the primary modified asphalt generates α -modification reaction and beta-modification reaction in the 2# reaction kettle 10 and simultaneously performs secondary modification reaction, flash evaporation oil gas generated by flash evaporation cracking is discharged to a stripping tower through a flash evaporation oil gas outlet at the top of the 2# reaction kettle 10, and the secondary modified asphalt after the secondary modification reaction fully flows into the 2# full-flow buffer tank 11 through an asphalt full-flow port;
4) the secondary modified asphalt in the 2# full flow buffer tank 11 is pumped out from the bottom by a 2# asphalt circulating pump 12, then is mixed with the primary modified asphalt, and a part of the secondary modified asphalt is sent to a 2# tubular furnace 13 to be heated and then is circularly sent back to the 2# reaction kettle 10; and the residual mixed modified asphalt is sent to a stripping tower through a modified asphalt conveying pipeline II, and the modified asphalt finished product is obtained after the stripping of the stripping tower.
The weight of the primary modified asphalt in the 1# full flow buffer tank 2 is monitored through the 1# weighing module 7 and the weight display controller-WRC 01, the weight is kept constant through the flow regulating valve-8, namely, the asphalt liquid level in the 1# full flow buffer tank 2 is kept constant, and on the basis, the extracted primary modified asphalt is sent to the second asphalt circulation loop to carry out secondary modification reaction.
The weight of the secondary modified asphalt in the 2# full-flow buffer tank 11 is monitored by the 2# weighing module 14 and the weight display controller WRC02, the weight is kept constant by the second flow control valve 15, namely, the asphalt liquid level in the 2# full-flow buffer tank 11 is kept constant, and the extracted secondary modified asphalt is sent to the stripping tower on the basis.
When a plurality of asphalt full flow ports are arranged, the height of the asphalt full flow port for discharging is selected according to the amount of the raw material asphalt in the 1/2# reaction kettle 10 of the 1# reaction kettle, and the full flow valve I9/the full flow valve II 16 controls the full flow discharging from the corresponding asphalt full flow port.
The utility model discloses in, for making 1# reation kettle 1, 2# reation kettle 10 can control the reaction dwell time of modified pitch through the full flow height, the middle part of 2 reation kettle 1, 10 sets up a flexible baffle 5 respectively, separates 1# reation kettle 1/2# reation kettle 10 into 2 reaction area territories, and the pitch flow channel intercommunication through flexible baffle 5 below between 2 reaction area territories. The asphalt feeding port is arranged above the reaction area at one side, and the asphalt full flow port is arranged above the reaction area at the other side, so that the asphalt is firstly fed in first out, and then fed out in last in the reaction kettles 1 and 10, and the reaction residence time of the asphalt is ensured. The flexible baffle 5 can also play a role in heat exchange, so that the temperature of the materials in the whole reaction kettles 1 and 10 is balanced, and the reaction efficiency is improved; the preferred cross-sectional shape of the flexible baffle 5 is a serpentine metal plate, and the serpentine cross-section enables the metal plate to have flexibility and large heat exchange area.
In order to control the stable amount of asphalt flowing out of the 1/2# reaction kettle 10 of the 1# reaction kettle, a full flow buffer tank 2/11 is added at the asphalt discharging end, and the outflow amount of the asphalt in the 1/10 # reaction kettle is controlled by controlling the stable liquid level of the full flow buffer tank 2/11; the full flow buffer tank 2/11 adopts a vertical small storage tank with 2 support lugs, the weighing module 7/14 is used for weighing, and the weight is converted into the liquid level, and the full flow buffer tank 2/11 is only provided with 2 support lugs, so that the accuracy and the stability of the measurement of the weighing module 7/14 can be ensured.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (3)
1. A system for producing modified asphalt by double-furnace double-kettle stripping flash evaporation is characterized by comprising a No. 1 reaction kettle, a No. 1 full-flow buffer tank, a No. 1 tubular furnace, a first asphalt circulation loop, a No. 2 reaction kettle, a No. 2 full-flow buffer tank, a No. 2 tubular furnace and a second asphalt circulation loop; the middle parts of the 1# reaction kettle and the 2# reaction kettle are respectively provided with a flexible baffle with a snake-shaped cross section, the 1# reaction kettle/the 2# reaction kettle is divided into 2 independent reaction areas, and the 2 reaction areas are communicated through an asphalt flow channel below the flexible baffle; an asphalt feeding hole is formed in the upper portion of the No. 1 reaction kettle/No. 2 reaction kettle on one side of the flexible baffle, and an asphalt full-flow port is formed in the upper portion of the No. 1 reaction kettle/No. 2 reaction kettle on the other side of the flexible baffle; a first asphalt circulation loop is arranged between an asphalt full-flow port and an asphalt feed port of the No. 1 reaction kettle, and a No. 1 full-flow buffer tank, a No. 1 asphalt circulation pump, an asphalt outflow port I, an asphalt inflow port I and a No. 1 tubular furnace are sequentially arranged on the first asphalt circulation loop along the asphalt conveying direction; wherein the asphalt inflow port I is connected with an external raw asphalt conveying pipeline; a second asphalt circulation loop is arranged between an asphalt full-flow port and an asphalt feeding port of the No. 2 reaction kettle, and a No. 2 full-flow buffer tank, a No. 2 asphalt circulation pump, an asphalt inflow port II, an asphalt outflow port II and a No. 2 tubular furnace are sequentially arranged on the second asphalt circulation loop along the asphalt conveying direction; the first asphalt outflow port on the first asphalt circulation loop is connected with the second asphalt inflow port on the second asphalt circulation loop through the first asphalt conveying pipeline, and the second asphalt outflow port on the second asphalt circulation loop is connected with the asphalt inlet of the stripping tower through the second asphalt conveying pipeline; the flash evaporation oil gas outlet at the top of the No. 1 reaction kettle and the flash evaporation oil gas outlet at the top of the No. 2 reaction kettle are connected with the oil gas inlet of the stripping tower through flash evaporation oil gas conveying pipelines.
2. The system for producing the modified asphalt by the double-furnace double-kettle stripping and flash evaporation as claimed in claim 1, wherein the No. 1 reaction kettle is provided with a plurality of asphalt full flow ports along the height direction, each asphalt full flow port is respectively connected with the first asphalt circulation loop through a full flow pipe I, and the full flow pipe I is respectively provided with a full flow valve I; and the No. 2 reaction kettle is provided with a plurality of asphalt full-flow ports along the height direction, each asphalt full-flow port is respectively connected with a second asphalt circulation loop through a full-flow pipe II, and the full-flow pipes II are respectively provided with a full-flow valve II.
3. The system for producing the modified asphalt by the double-furnace double-kettle stripping and flash evaporation as claimed in claim 1, wherein a first flow control valve is arranged at the upstream of the first asphalt conveying pipeline, the 1# full-flow buffer tank is supported on a 1# weighing module through 2 support lugs, and the 1# weighing module is connected with the first flow control valve through a weight display controller; and a second flow regulating valve is arranged at the upstream of the second asphalt conveying pipeline, the 2# full-flow buffer tank is supported on the 2# weighing module through 2 support lugs, and the 2# weighing module is connected with the second flow regulating valve through a second weight display controller.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921145449.1U CN210560259U (en) | 2019-07-19 | 2019-07-19 | System for producing modified asphalt by double-furnace double-kettle stripping flash evaporation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921145449.1U CN210560259U (en) | 2019-07-19 | 2019-07-19 | System for producing modified asphalt by double-furnace double-kettle stripping flash evaporation |
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| CN210560259U true CN210560259U (en) | 2020-05-19 |
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| CN201921145449.1U Withdrawn - After Issue CN210560259U (en) | 2019-07-19 | 2019-07-19 | System for producing modified asphalt by double-furnace double-kettle stripping flash evaporation |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240918A (en) * | 2019-07-19 | 2019-09-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of system and technique of the double kettle stripping flash distillation production modified coal tar pitches of twin furnace |
-
2019
- 2019-07-19 CN CN201921145449.1U patent/CN210560259U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110240918A (en) * | 2019-07-19 | 2019-09-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of system and technique of the double kettle stripping flash distillation production modified coal tar pitches of twin furnace |
| 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 |
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