CN218146497U - Tar treatment fractionating tower system - Google Patents
Tar treatment fractionating tower system Download PDFInfo
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- CN218146497U CN218146497U CN202222245799.3U CN202222245799U CN218146497U CN 218146497 U CN218146497 U CN 218146497U CN 202222245799 U CN202222245799 U CN 202222245799U CN 218146497 U CN218146497 U CN 218146497U
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Abstract
The utility model discloses a tar processing fractionating tower system, including the fractionating tower of tar decompression processing, the top of the tower of fractionating tower overflows the phenol naphthalene wash three thoughtlessly cut through three thoughtlessly oily heat exchangers and the preliminary cooling back of raw materials tar heat transfer, again through three thoughtlessly oily gas cooler condensation cooling back liquid gets into three thoughtlessly oily return channels, three thoughtlessly oily return channels inside fractionation divide to send back the fraction top of the tower as the backward flow processing through the backwash pump, the utility model discloses a set up the liquid seal high enough vacuum water seal jar and can compensate the liquid seal of three thoughtlessly oily return channels in can not seal the fractionating tower to the vacuum system pressure requirement that three thoughtlessly oily gas cooler to the vacuum pump is constituteed, fundamentally has stopped three thoughtlessly oily gas cooling's noncondensable gas band liquid and has got into the vacuum system phenomenon, has both guaranteed the negative pressure operation of fractionating tower, has guaranteed three thoughtlessly oily return channels malleation operation again, has solved three thoughtlessly oily return pumps backwash pump non-up or the volume unstability, and has shaken the serious problem, has stabilized the quality of three thoughtlessly oily products.
Description
Technical Field
The utility model relates to a chemical industry tar field of handling, concretely relates to fraction tower system is handled to tar.
Background
The distillation process of tar treatment mainly adopts a tower type tar continuous distillation process of cutting mixed fractions by vacuum distillation, which is an advanced technology for treating tar in China.
In the conventional vacuum distillation system for treating tar (as shown in FIG. 2), the pressure at the top of a fractionating tower 1 is controlled to be 15-20 kPa, and the temperature is controlled to be 160-175 ℃. After the phenol naphthalene washing three-mixed fraction oil gas escaping from the top of the fractionating tower 1 is subjected to heat exchange and primary cooling with raw material tar through a three-mixed oil heat exchanger 2, and then is condensed and cooled through a three-mixed oil cooler 3, liquid enters a three-mixed oil reflux tank 4, part of fraction is returned to the top of the fractionating tower through a reflux pump 5 to be used as reflux, the rest fraction is sent to a three-mixed fraction tank 6, and the fraction in the three-mixed fraction tank 6 is sent to a fraction alkali washing unit to be washed and dephenolized;
the tower top negative pressure system of the fractionating tower 1 is formed by the negative pressure pumped by the vacuum pump 9. The non-condensable gas of the three-mixed oil cooler 3 is continuously pumped out by the vacuum pump 9 at the upper part of the three-mixed oil cooler, but in the operation, the three-mixed oil reflux pump 5 can not pump up or the liquid in the three-mixed oil reflux tank 4 is unstable, and an outlet regulating valve and a flow meter of the reflux pump 5 are seriously shaken to form circulation, so that the three-mixed oil product is unqualified.
Subsequent investigation finds that the pressure of a buffer tank at the inlet of the vacuum pump 9 is-57.4 kpa, the pressure of the top of the fractionating tower is-31.2 kpa, the liquid level in the three-mixed oil reflux tank is about 786mm (about 7-8 kpa), the negative pressure of the vacuum pump is high, the liquid level of the three-mixed oil reflux tank 4 is low, a liquid seal formed in the three-mixed oil reflux tank 4 cannot seal a vacuum system formed by the fractionating tower 1 to the three-mixed oil cooler 3 to the vacuum pump 9, and the phenomenon that the non-condensable gas of the three-mixed oil cooler 3 carries liquid to enter the vacuum system is caused, so that the three-mixed oil reflux pump 5 cannot pump or the three-mixed oil reflux pump 5 is unstable in pumping, and an outlet regulating valve and a flow meter of the reflux pump 5 are seriously shaken, so that the three-mixed oil product is unqualified.
SUMMERY OF THE UTILITY MODEL
In order to solve the existing problems, the utility model provides a tar treatment fractionating tower system.
The utility model discloses a realize through following technical scheme:
a tar treatment fractionating tower system comprises a fractionating tower for tar decompression treatment, wherein a phenol naphthalene washing three-mixed fraction escaped from the tower top of the fractionating tower is subjected to preliminary cooling with raw material tar through a three-mixed oil heat exchanger, then the phenol naphthalene washing three-mixed fraction is condensed and cooled by a three-mixed oil cooler, then liquid enters a three-mixed oil reflux tank, a fractionation branch inside the three-mixed oil reflux tank is sent back to the top of the fractionating tower through a reflux pump to be treated as reflux, other fractions in the three-mixed oil reflux tank are sent to the three-mixed fraction tank to be cached, a negative pressure system is arranged on the top of the fractionating tower, and a vacuum water-sealed tank for stabilizing system operation is arranged between a condensate outlet of the three-mixed oil cooler and an inlet of the three-mixed oil reflux tank.
Further optionally, the negative pressure system continuously pumps the non-condensable gas at the upper part in the three-oil-mixed gas cooler through a pipeline by using a vacuum pump so as to integrally realize the negative pressure operation of the fractionating tower, the three-oil-mixed heat exchanger and the three-oil-mixed gas cooler.
Further optionally, the negative pressure system comprises a buffer tank and a vacuum pump which are connected with each other, and an inlet of the buffer tank is connected with the upper part of the three-mixed oil gas cooler through a pipeline.
Further optionally, the vacuum water-sealed tank comprises a sleeve and an internal liquid inlet pipe, an inlet of the liquid inlet pipe is connected with the lower part of the three-mixed oil gas cooler through a drainage pipe, and a side end of the top of the sleeve is connected with an inlet of the three-mixed oil reflux groove through a reflux pipe.
Further optionally, the draft tube is arranged along the three-mix oil cooler inclined downwards towards the vacuum water-sealed tank.
Further optionally, the pressure value converted by the liquid seal height of the vacuum water seal tank is greater than the pressure value in the buffer tank.
Further optionally, control valves are respectively installed on a pipeline connected between the fractionating tower, the three-mixed oil heat exchanger, the three-mixed oil cooler, the three-mixed oil reflux tank, the reflux pump and the three-mixed distillate tank, and on the drainage pipe and the reflux pipe.
Compared with the prior art, the beneficial effects of the utility model are that: the utility model discloses a set up the liquid seal highly sufficient vacuum water seal tank and can compensate the liquid seal in the three oil mixing reflux grooves and can not seal the fractionating tower to the vacuum system pressure requirement that three oil mixing gas cooler to vacuum pump are constituteed, fundamentally has stopped three oil mixing gas cooler's noncondensable gas and has taken the liquid to get into the vacuum system phenomenon, the negative pressure operation of fractionating tower has both been guaranteed, three oil mixing reflux grooves malleation operations has been guaranteed again, three oil mixing reflux pumps are not upper to measure or the upper to measure unstability has been solved, the backwash pump export governing valve, the serious problem of flowmeter shake, the quality of three oil mixing products has been stabilized.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention;
FIG. 2 is a prior art system diagram of the present application;
in the figure: the system comprises a fractionating tower 1, a three-mixed oil heat exchanger 2, a three-mixed oil cooler 3, a three-mixed oil reflux tank 4, a reflux pump 5, a three-mixed fractionation tank 6, a negative pressure pipeline 7, a buffer tank 8, a vacuum pump 9, a drainage tube 10, a liquid inlet tube 11, a sleeve 12 and a reflux tube 13.
Detailed Description
The present invention will be described in further detail with reference to the following detailed description and accompanying drawings:
as shown in fig. 1, a distillate tower system for tar treatment comprises a distillate tower 1 for tar decompression treatment, wherein the trinary mixed fraction of phenol naphthalene washing escaping from the top of the distillate tower 1 is subjected to heat exchange with raw tar through a trinary mixed oil heat exchanger 2 for primary cooling, and then is condensed and cooled by a trinary mixed oil cooler 3, and then liquid enters a trinary mixed oil reflux tank 4, the fraction in the trinary mixed oil reflux tank 4 is returned to the top of the distillate tower 1 through a reflux pump 5 for reflux treatment, the rest fractions in the trinary mixed oil reflux tank 4 are sent to a trinary mixed fraction tank 6 for caching, a negative pressure system is arranged at the top of the distillate tower 1, and a vacuum water-sealed tank for stabilizing system operation is arranged between a condensate outlet of the trinary mixed oil cooler 3 and an inlet of the trinary mixed oil reflux tank 4.
As shown in fig. 1, the negative pressure system continuously pumps the non-condensable gas at the upper part in the three-oil-mixed gas cooler 3 through a pipeline by a vacuum pump 9 so as to integrally realize the negative pressure operation of the fractionating tower 1, the three-oil-mixed heat exchanger 2 and the three-oil-mixed gas cooler 3.
As shown in fig. 1, the negative pressure system comprises a buffer tank 8 and a vacuum pump 9 which are connected with each other, and an inlet of the buffer tank 8 is connected with the upper part of the three-in-one oil cooler 3 through a pipeline.
As shown in FIG. 1, the vacuum water-sealed tank comprises a sleeve 12 and an internal liquid inlet pipe 11, wherein an inlet of the liquid inlet pipe 11 is connected with the lower part of the three-mixed oil gas cooler 3 through a drainage pipe 10, and a top side end of the sleeve 12 is connected with an inlet of the three-mixed oil return tank 4 through a return pipe 13.
As shown in fig. 1, the drainage tube 10 is arranged along the three-mixed oil gas cooler 3 and inclined downwards to the vacuum water sealed tank, so that the liquid in the three-mixed oil gas cooler 3 is ensured to enter the vacuum water sealed tank all the time, and the liquid sealing height of the vacuum water sealed tank is ensured.
As shown in fig. 1, the liquid seal height of the vacuum water-sealed tank is converted into a pressure value larger than the pressure value in the buffer tank 8, so that the liquid seal effect can be ensured even when the vacuum pump pressure is maximum.
As shown in fig. 1, control valves are respectively installed on pipelines connected between a fractionating tower 1, a three-mixed oil heat exchanger 2, a three-mixed oil cooler 3, a three-mixed oil reflux tank 4, a reflux pump 5 and a three-mixed fraction tank 6, and on a drainage tube 10 and a reflux tube 13, and the control valves are arranged to control the stable operation of the system.
The implementation principle of the tar treatment fractionating tower system in the embodiment of the application is as follows: after the phenol naphthalene washing tertiary mixed fraction escaped from the top of the fractionating tower 1 is subjected to heat exchange with raw material tar through a tertiary mixed oil heat exchanger 2 and is subjected to primary temperature reduction, the condensed and cooled liquid of the tertiary mixed oil gas cooler 3 enters a liquid inlet pipe 11 of a vacuum water-sealed tank through a drainage pipe 10, a liquid seal is formed in a sleeve 12 of the vacuum water-sealed tank, and finally the liquid enters a tertiary mixed oil reflux tank 4 along a reflux pipe 13 for subsequent circulation treatment;
the set liquid seal height conversion pressure value of the vacuum water seal tank is larger than 8 pressure values-57.4 Kpa (10 Kpa pressure is equal to the height of 1 liquid) of a buffer tank of a vacuum pump 9, namely the liquid seal height of the vacuum water seal tank is larger than 6000mm, so that the vacuum water seal tank can not be broken under the pressure of the maximum vacuum pump 9, and the liquid seal effect is ensured;
the vacuum water-sealed tank arranged like this can make up the pressure requirement of a vacuum system formed by the distillation tower 1 to the three-mixed oil gas cooler 3 to the vacuum pump 9, which can not be sealed by the liquid seal in the three-mixed oil reflux tank 4, thereby fundamentally preventing the phenomenon that the non-condensable gas of the three-mixed oil gas cooler 3 enters the vacuum system with the liquid, not only ensuring the negative pressure operation of the distillation tower 1, but also ensuring the positive pressure operation of the three-mixed oil reflux tank 4, solving the problems that the three-mixed oil reflux pump 5 is not or not stable in upper amount, the outlet regulating valve of the reflux pump 5 and the flowmeter are seriously shaken, and stabilizing the quality of three-mixed oil products.
The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It should be understood by those skilled in the art that the present invention is not limited to the above embodiments, and the above embodiments and descriptions are only illustrative of the principles of the present invention, and that various changes and modifications may be made without departing from the spirit and scope of the present invention, and all such changes and modifications fall within the scope of the present invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (7)
1. The utility model provides a tar processing fractionating tower system, includes fractionating tower (1) to tar decompression processing, the top of the tower of fractionating tower (1) overflows the phenol naphthalene wash three thoughtlessly to be divided after three thoughtlessly oily heat exchanger (2) and the preliminary cooling of raw materials tar heat transfer, liquid gets into three thoughtlessly oily backward flow groove (4) after three thoughtlessly oily gas cooler (3) condensation cooling again, three thoughtlessly oily backward flow groove (4) inside is divided and is sent back to fractionating tower (1) top through backwash pump (5) and handle as the backward flow, all the other fractions send to three thoughtlessly to divide groove (6) and buffer memory in three thoughtlessly oily backward flow groove (4), its characterized in that: and a negative pressure system is arranged at the top of the fractionating tower (1), and a vacuum water seal tank for stabilizing the operation of the system is arranged between a condensate outlet of the three-mixed oil cooler (3) and an inlet of the three-mixed oil reflux tank (4).
2. The tar processing column system of claim 1, wherein: the negative pressure system continuously pumps non-condensable gas at the upper part in the three-mixed oil gas cooler (3) through a pipeline by a vacuum pump (9), so that the negative pressure operation of the fractionating tower (1), the three-mixed oil heat exchanger (2) and the three-mixed oil gas cooler (3) is integrally realized.
3. The tar processing column system of claim 2, wherein: the negative pressure system comprises a buffer tank (8) and a vacuum pump (9) which are connected with each other, wherein the inlet of the buffer tank (8) is connected with the upper part of the three-mixed oil gas cooler (3) through a pipeline.
4. The tar processing column system of claim 1, wherein: the vacuum water-sealed tank comprises a sleeve (12) and an internal liquid inlet pipe (11), the inlet of the liquid inlet pipe (11) is connected with the lower part of the three-mixed oil gas cooler (3) through a drainage pipe (10), and the top side end of the sleeve (12) is connected with the inlet of the three-mixed oil reflux groove (4) through a reflux pipe (13).
5. The tar processing column system of claim 4, wherein: the drainage tube (10) is arranged downwards along the three-mixed oil gas cooler (3) to the vacuum water-sealed tank.
6. The tar processing tower system according to claim 1, wherein: the pressure value of the liquid seal height conversion of the vacuum water seal tank is larger than the pressure value in the buffer tank (8).
7. The tar processing column system of claim 1, wherein: control valves are arranged on pipelines connected among the fractionating tower (1), the three-mixed oil heat exchanger (2), the three-mixed oil cooler (3), the three-mixed oil reflux groove (4), the reflux pump (5) and the three-mixed fractionating groove (6), as well as on the drainage tube (10) and the reflux tube (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222245799.3U CN218146497U (en) | 2022-08-25 | 2022-08-25 | Tar treatment fractionating tower system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222245799.3U CN218146497U (en) | 2022-08-25 | 2022-08-25 | Tar treatment fractionating tower system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218146497U true CN218146497U (en) | 2022-12-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222245799.3U Active CN218146497U (en) | 2022-08-25 | 2022-08-25 | Tar treatment fractionating tower system |
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| Country | Link |
|---|---|
| CN (1) | CN218146497U (en) |
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2022
- 2022-08-25 CN CN202222245799.3U patent/CN218146497U/en active Active
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