CN218755600U - Energy-saving coal tar processing system - Google Patents
Energy-saving coal tar processing system Download PDFInfo
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- CN218755600U CN218755600U CN202222880484.6U CN202222880484U CN218755600U CN 218755600 U CN218755600 U CN 218755600U CN 202222880484 U CN202222880484 U CN 202222880484U CN 218755600 U CN218755600 U CN 218755600U
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Abstract
The utility model relates to a heat recovery technical field in the petrochemical industry, concretely relates to energy-conserving moulded coal tar processing system. The heating system comprises a heavy anthracene oil/raw oil heat exchanger, a first middle section oil/raw oil heat exchanger, a second middle section oil/raw oil heat exchanger, a heavy oil/raw oil heat exchanger, a circulating oil/raw oil heat exchanger and a heating furnace I which are sequentially connected in series; a heavy anthracene oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the heavy anthracene oil/raw material oil heat exchanger; a middle section oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the middle section oil/raw material oil heat exchanger; a second middle section oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the second middle section oil/raw material oil heat exchanger; a heavy oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the heavy oil/raw oil heat exchanger; the circulating oil/raw oil heat exchanger is connected in a pipeline of a circulating oil system. The utility model provides an energy-saving coal tar processing system.
Description
Technical Field
The utility model relates to a heat recovery technical field in the petrochemical industry, concretely relates to energy-conserving moulded coal tar processing system.
Background
Coal tar is heated and then introduced into a raw material fractionating tower for prefractionation, the currently used process is that the coal tar is firstly introduced into a preheater, heated to 90 ℃ by using 1.0MPa steam, enters a raw material oil buffer tank, is heated by using a gas heating furnace and then enters a reduced pressure fractionating tower, and the consumption of steam and fuel in the process is large. The temperature of the materials fractionated from the raw material fractionating tower is high, the energy can not be utilized, and air cooling or water cooling is also needed, so that great energy waste is caused.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that the energy is wasted by the coal tar prefractionation process in the prior art, and provides an energy-saving coal tar processing system.
The utility model provides an above-mentioned technical problem's technical scheme as follows:
an energy-saving coal tar processing system comprises a raw oil storage tank, a heating system, a raw material fractionating tower and a circulating oil system, wherein the raw oil storage tank is connected with the raw material fractionating tower through the heating system, the product of the raw material fractionating tower comprises tower top oil, first middle oil, second middle oil, heavy anthracene oil and heavy oil, and is characterized in that,
the heating system comprises a heavy anthracene oil/raw oil heat exchanger, a first middle section oil/raw oil heat exchanger, a second middle section oil/raw oil heat exchanger, a heavy oil/raw oil heat exchanger, a circulating oil/raw oil heat exchanger and a heating furnace I which are sequentially connected in series;
a heavy anthracene oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the heavy anthracene oil/raw material oil heat exchanger through a pipeline and a pump I; a middle section oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the middle section oil/raw material oil heat exchanger through a pipeline and a pump II; a second middle section oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the second middle section oil/raw material oil heat exchanger through a pipeline and a pump III; a heavy oil outlet of the raw material fractionating tower is connected with a heat exchange medium inlet of the heavy oil/raw oil heat exchanger through a pipeline and a pump IV; and the heat exchange medium inlet and the heat exchange medium outlet of the circulating oil/raw oil heat exchanger are connected in a pipeline of a circulating oil system.
Further, the device also comprises a hydrofining cracking device and a product fractionating tower; the tower top oil pipeline, the heat exchange medium outlet of the first middle section oil/raw oil heat exchanger and the heat exchange medium outlet of the second middle section oil/raw oil heat exchanger are all connected to a mixing tank, the mixing tank is connected to a hydrofining and cracking device through pipelines, and the heat exchange medium outlet of the heavy anthracene oil/raw oil heat exchanger is connected to the hydrofining and cracking device through pipelines; the hydrocracking unit is connected to the product fractionation column via a pipeline.
Further, the circulating oil system comprises a heater at the bottom of the product fractionating tower, the outlet end of the heater at the bottom of the product fractionating tower is connected with a circulating pump, and the outlet end of the circulating pump is connected with a three-way pipe; one branch pipe of the three-way pipe is connected with a heating furnace II, an outlet of the heating furnace II is connected to an inlet of a heater at the bottom of the product fractionating tower, the other branch pipe of the three-way pipe is sequentially connected with a circulating oil/raw oil heat exchanger and a circulating oil storage tank through pipelines, and the circulating oil storage tank is connected to an inlet of the heater at the bottom of the product fractionating tower.
Furthermore, an anthracene oil storage tank is connected in a pipeline between a heat exchange medium outlet of the heavy anthracene oil/raw oil heat exchanger and the hydrofining and cracking device.
Furthermore, a parallel connection pipeline which can be switched to use with the heavy anthracene oil/raw oil heat exchanger is also arranged on a pipeline between the heat exchange medium outlet of the heavy anthracene oil/raw oil heat exchanger and the heavy anthracene oil storage tank, and an air cooler is arranged in the parallel connection pipeline.
Further, a water cooling device I is connected between a heat exchange medium outlet of the middle section oil/raw oil heat exchanger and the mixing tank; and a water cooling device II is connected between the heat exchange medium outlet of the second middle section oil/raw oil heat exchanger and the mixing tank.
Further, a heat exchange medium outlet of the heavy oil/raw oil heat exchanger is connected with a heavy oil storage tank.
The utility model has the advantages that:
the utility model discloses a set up heating system and include heavy anthracene oil/raw oil heat exchanger, one middle section oil/raw oil heat exchanger, two middle sections oil/raw oil heat exchangers, heavy oil/raw oil heat exchanger, cycle oil/raw oil heat exchanger and the heating furnace I that serially connect in proper order, utilize the output and the cycle oil of raw materials fractionating tower to heat the raw oil and heat up, realize thermal recycle, energy saving and consumption reduction;
on the other hand, the heavy anthracene oil, the first middle oil and the second middle oil need to be cooled after coming out of the raw material fractionating tower, the temperature of the components of the device is reduced after heat exchange through a heat exchanger, for example, the heavy anthracene oil needs to be cooled by a plurality of air coolers originally, and one air cooler may need to be started only under the condition of high environmental temperature in summer; the device effectively reduces the investment of enterprise cooling equipment and energy, and reduces the production cost.
Drawings
Fig. 1 is a schematic structural diagram of the present invention;
in the figure: 1. the system comprises a raw oil storage tank, 2. A heavy anthracene oil/raw oil heat exchanger, 3. A first middle oil/raw oil heat exchanger, 4. A second middle oil/raw oil heat exchanger, 5. A heavy oil/raw oil heat exchanger, 6. A circulating oil/raw oil heat exchanger, 7. A heating furnace I, 8. A raw material fractionating tower, 9. A hydrofining cracking device, 10. A product fractionating tower, 11. An air cooler, 12. A mixing tank, 13. A heavy oil storage tank, 14. A circulating oil storage tank, 15. A heavy anthracene oil storage tank, 16. A circulating pump, 17. A heating furnace II, 18. A pump I, 19. A pump II, 20. A pump III, 21. A pump IV.
Detailed Description
The principles and features of the present invention will be described with reference to the drawings, which are provided for illustration purposes only and are not intended to limit the scope of the present invention.
As shown in fig. 1, the energy-saving coal tar processing system of the embodiment includes a raw oil storage tank 1, a heating system, a raw material fractionating tower 8, a hydrorefining cracking device 9, a product fractionating tower 10 and a circulating oil system, the raw oil storage tank 1 is connected with the raw material fractionating tower 8 through the heating system, and the product of the raw material fractionating tower 8 includes top oil, first middle oil, second middle oil, heavy anthracene oil and heavy oil. The tower top oil, the first middle oil and the second middle oil are mixed to be called light anthracene oil. Light anthracene oil and heavy anthracene oil are treated by a hydrofining cracking device 9 and enter a product fractionating tower 10 for fractionation.
The heating system comprises a heavy anthracene oil/raw oil heat exchanger 2, a first middle section oil/raw oil heat exchanger 3, a second middle section oil/raw oil heat exchanger 4, a heavy oil/raw oil heat exchanger 5, a circulating oil/raw oil heat exchanger 6 and a heating furnace I7 which are sequentially connected in series.
A heavy anthracene oil outlet of the raw material fractionating tower 8 is connected with a heat exchange medium inlet of the heavy anthracene oil/raw material oil heat exchanger 2 through a pipeline and a pump I18; the outlet of the heat exchange medium of the heavy anthracene oil/raw oil heat exchanger 2 is connected to a hydrofining cracking device 9 through a pipeline; the hydrocracking apparatus is connected to the product fractionation column 10 through a pipe. Further, an anthracene oil storage tank is connected in a pipeline between a heat exchange medium outlet of the heavy anthracene oil/raw oil heat exchanger 2 and the hydrofining and cracking device 9, a parallel pipeline capable of being switched for use with the heavy anthracene oil storage tank is further arranged on the pipeline between the heat exchange medium outlet of the heavy anthracene oil/raw oil heat exchanger 2 and the heavy anthracene oil storage tank 15, and an air cooler 11 is arranged in the parallel pipeline. Whether to turn on the air cooler 11 may be selected as desired.
A middle section oil outlet of the raw material fractionating tower 8 is connected with a heat exchange medium inlet of the middle section oil/raw material oil heat exchanger 3 through a pipeline and a pump II 19; and a second middle section oil outlet of the raw material fractionating tower 8 is connected with a heat exchange medium inlet of the second middle section oil/raw material oil heat exchanger 4 through a pipeline and a pump III 20.
The tower top oil pipeline, the heat exchange medium outlet of the first middle section oil/raw oil heat exchanger 3 and the heat exchange medium outlet of the second middle section oil/raw oil heat exchanger 4 are all connected to a mixing tank 12, and the mixing tank 12 is connected to the hydrofining cracking device 9 through pipelines. Preferably, a water cooling device I is connected between the heat exchange medium outlet of the middle section oil/raw oil heat exchanger 3 and the mixing tank 12; a water cooling device II is connected between the heat exchange medium outlet of the second middle section oil/raw oil heat exchanger 4 and the mixing tank 12, and whether the water cooling device I and the water cooling device II (not shown in the figure) are used or not can be selected according to the temperature of the first middle section oil and the second middle section oil after heat exchange. It can be understood that if the temperature of the oil in the first middle section and the oil in the second middle section after heat exchange can meet the standard, the water cooling equipment I and the water cooling equipment II do not need to be arranged.
A heavy oil outlet of the raw material fractionating tower 8 is connected with a heat exchange medium inlet of the heavy oil/raw oil heat exchanger 5 through a pipeline and a pump IV 21; and a heavy oil storage tank 13 is connected to a heat exchange medium outlet of the heavy oil/raw oil heat exchanger 5.
And the heat exchange medium inlet and the heat exchange medium outlet of the circulating oil/raw oil heat exchanger 6 are connected in a pipeline of a circulating oil system. Specifically, the circulating oil system comprises a heater at the bottom of the product fractionating tower 10, the outlet end of the heater at the bottom of the product fractionating tower 10 is connected with a circulating pump 16, and the outlet end of the circulating pump 16 is connected with a three-way pipe; one branch pipe of the three-way pipe is connected with a heating furnace II, the outlet of the heating furnace II is connected to the inlet of the heater at the bottom of the product fractionating tower 10, the other branch pipe of the three-way pipe is sequentially connected with a circulating oil/raw oil heat exchanger 6 and a circulating oil storage tank 14 through pipelines, and the circulating oil storage tank 14 is connected to the inlet of the heater at the bottom of the product fractionating tower 10. Optionally, a reboiler of the product fractionation column 10 is connected between the recycle oil storage tank 14 and an inlet of a heater at the bottom of the product fractionation column 10, and the recycle oil provides heat energy to the reboiler.
The utility model discloses a set up heating system including the heavy anthracene oil/raw oil heat exchanger 2, a middle section oil/raw oil heat exchanger 3, two middle sections oil/raw oil heat exchangers 4, heavy oil/raw oil heat exchanger 5, cycle oil/raw oil heat exchanger 6 and the heating furnace I7 that serially connect in proper order, utilize the output and the cycle oil of raw materials fractionating tower 8 to heat raw oil and heat up, realize energy saving and consumption reduction to thermal recycle. Raw oil is heated by a heating system without needing steam, the steam temperature of 1.0MPa is generally between 160 and 220 ℃, the external production temperature of heavier anthracene oil is much lower than 320 ℃, the heat exchange between the heavy anthracene oil and the raw oil is more sufficient, the raw oil feeding temperature can be effectively improved, the steam consumption is saved by about 0.8t/h, the influence on the device production caused by the stop or reduction of the steam is avoided, the possibility of operating the steam by personnel is avoided to a certain extent, and the operation risk is reduced.
On the other hand, the heavy anthracene oil, the first-stage oil and the second-stage oil need to be cooled after coming out of the raw material fractionating tower 8, the temperature of the components of the device is reduced after heat exchange through a heat exchanger, for example, the heavy anthracene oil needs to be cooled by a plurality of air coolers 11 originally, and one air cooler 11 may be started under the condition of high environmental temperature in summer; the device effectively reduces the investment of enterprise cooling equipment and energy, and reduces the production cost.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications can be made without departing from the scope of the invention.
Claims (7)
1. An energy-saving coal tar processing system comprises a raw oil storage tank (1), a heating system, a raw material fractionating tower (8) and a circulating oil system, wherein the raw oil storage tank (1) is connected with the raw material fractionating tower (8) through the heating system, the product of the raw material fractionating tower (8) comprises tower top oil, first middle oil, second middle oil, heavy anthracene oil and heavy oil, and is characterized in that,
the heating system comprises a heavy anthracene oil/raw oil heat exchanger (2), a first middle section oil/raw oil heat exchanger (3), a second middle section oil/raw oil heat exchanger (4), a heavy oil/raw oil heat exchanger (5), a circulating oil/raw oil heat exchanger (6) and a heating furnace I (7) which are sequentially connected in series;
a heavy anthracene oil outlet of the raw material fractionating tower (8) is connected with a heat exchange medium inlet of the heavy anthracene oil/raw material oil heat exchanger (2) through a pipeline and a pump I (18); a middle section oil outlet of the raw material fractionating tower (8) is connected with a heat exchange medium inlet of the middle section oil/raw material oil heat exchanger (3) through a pipeline and a pump II (19); a second middle section oil outlet of the raw material fractionating tower (8) is connected with a heat exchange medium inlet of the second middle section oil/raw material oil heat exchanger (4) through a pipeline and a pump III (20); a heavy oil outlet of the raw material fractionating tower (8) is connected with a heat exchange medium inlet of the heavy oil/raw oil heat exchanger (5) through a pipeline and a pump IV (21); and the heat exchange medium inlet and the heat exchange medium outlet of the circulating oil/raw oil heat exchanger (6) are connected in a pipeline of a circulating oil system.
2. The energy-saving coal tar processing system according to claim 1, further comprising a hydrofining and cracking device (9) and a product fractionating tower (10);
the tower top oil pipeline, the heat exchange medium outlet of the first middle section oil/raw oil heat exchanger (3) and the heat exchange medium outlet of the second middle section oil/raw oil heat exchanger (4) are connected to a mixing tank (12), the mixing tank (12) is connected to a hydrofining cracking device (9) through a pipeline, and the heat exchange medium outlet of the heavy anthracene oil/raw oil heat exchanger (2) is connected to the hydrofining cracking device (9) through a pipeline; the hydrocracking unit is connected to a product fractionation column (10) through a pipe.
3. The energy-saving coal tar processing system according to claim 1, wherein the circulating oil system comprises a heater at the bottom of the product fractionating tower (10), the outlet end of the heater at the bottom of the product fractionating tower (10) is connected with a circulating pump (16), and the outlet end of the circulating pump (16) is connected with a three-way pipe; one branch pipe of the three-way pipe is connected with a heating furnace II, an outlet of the heating furnace II is connected to an inlet of a tower bottom heater of the product fractionating tower (10), the other branch pipe of the three-way pipe is sequentially connected with a circulating oil/raw oil heat exchanger (6) and a circulating oil storage tank (14) through pipelines, and the circulating oil storage tank (14) is connected to an inlet of the tower bottom heater of the product fractionating tower (10).
4. The energy-saving coal tar processing system according to claim 2 or 3, wherein an anthracene oil storage tank is connected in a pipeline between the outlet of the heat exchange medium of the heavy anthracene oil/raw oil heat exchanger (2) and the hydrofining and cracking device (9).
5. The energy-saving coal tar processing system according to claim 4, wherein a parallel pipeline which can be switched to use with the heavy anthracene oil/raw oil heat exchanger (2) is arranged on a pipeline between the heat exchange medium outlet and the heavy anthracene oil storage tank (15), and an air cooler (11) is arranged in the parallel pipeline.
6. The energy-saving coal tar processing system according to claim 2 or 3, wherein a water cooling device I is connected between the heat exchange medium outlet of the middle section oil/raw oil heat exchanger (3) and the mixing tank (12); a water cooling device II is connected between the heat exchange medium outlet of the second middle section oil/raw oil heat exchanger (4) and the mixing tank (12).
7. The energy-saving coal tar processing system according to claim 2 or 3, wherein the outlet of the heat exchange medium of the heavy oil/raw oil heat exchanger (5) is connected with a heavy oil storage tank (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222880484.6U CN218755600U (en) | 2022-10-31 | 2022-10-31 | Energy-saving coal tar processing system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222880484.6U CN218755600U (en) | 2022-10-31 | 2022-10-31 | Energy-saving coal tar processing system |
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| Publication Number | Publication Date |
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| CN218755600U true CN218755600U (en) | 2023-03-28 |
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| CN202222880484.6U Active CN218755600U (en) | 2022-10-31 | 2022-10-31 | Energy-saving coal tar processing system |
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