CN213977550U - Rich oil debenzolization heating system - Google Patents
Rich oil debenzolization heating system Download PDFInfo
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- CN213977550U CN213977550U CN202022558723.7U CN202022558723U CN213977550U CN 213977550 U CN213977550 U CN 213977550U CN 202022558723 U CN202022558723 U CN 202022558723U CN 213977550 U CN213977550 U CN 213977550U
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- pipeline
- debenzolization
- heat exchanger
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Abstract
The utility model provides a rich oil debenzolization heating system, which comprises a heat exchanger, the fluid inlet connection rich oil inlet pipe that is heated of heat exchanger, the fluid outlet connection rich oil outlet pipe that is heated of heat exchanger, the other end of rich oil outlet pipe is connected to on the debenzolization tower, be provided with temperature sensor on the rich oil outlet pipe, the superheated steam pipeline of heat transfer fluid access connection of heat exchanger, the other end and the steam boiler of superheated steam pipeline are connected, the heat transfer fluid exit linkage condensate pipe of heat exchanger, the other end of condensate pipe is connected to on the low pressure flash tank. The heating system has the advantages of small occupied area, safety, environmental protection, no generation of gases such as sulfur, nitrogen oxides and the like, no danger of burning coal gas, cost saving and economic benefit improvement.
Description
Technical Field
The utility model relates to a rich oil debenzolization system specifically says so and relates to a rich oil debenzolization heating system.
Background
In the current rich oil debenzolization technology in an industrial coal chemical system, the rich oil is heated by adopting a tubular furnace, the tubular furnace is used for heating the rich oil at 120 ℃ to 180 ℃ and then entering a debenzolization tower for debenzolization, and a combustion medium is combusted in the tubular furnaceThe coal gas is burnt in a hearth of a tubular furnace, the burnt flue gas contains harmful substances such as sulfur dioxide, nitrogen oxide and the like, and the coke oven gas contains 100mg/m of sulfur3200mg of S0 produced by burning coke oven gas per cubic meter2The gas combustion consumption of the tubular furnace per hour is 2400m3Hourly production of S020.48kg of S0, 4204kg of S0 are produced each year2Each chemical plant has at least 4 such tube furnaces, and the next chemical plant tube furnace discharge S0 is calculated216.8 tons, and most of the flue gas after burning in the tubular furnace of the coke-oven plant is not purified and is directly discharged through a chimney, thus polluting the environment, and the cost is higher when the flue gas of the tubular furnace is treated. Moreover, the tubular furnace has low heating thermal efficiency of about 70 percent, a large amount of coal gas is wasted, and the economic benefit is poor. The tubular furnace adopts coke oven gas as fuel, the coke oven gas is an inflammable, explosive and toxic medium during open fire operation, the operation is strictly carried out according to the operation regulations during the operation, and the fire and explosion accidents are easily caused due to improper operation. The tube furnace has strict safety spacing with class A media (crude benzene) and other equipment and buildings, and the tube furnace has larger equipment volume, large occupied area and poor site utilization rate.
Disclosure of Invention
In order to overcome the defects in the prior art, the utility model provides a rich oil debenzolization heating system.
The utility model discloses a realize through following technical scheme: the utility model provides a rich oil debenzolization heating system, includes the heat exchanger, the fluid inlet connection rich oil inlet pipeline that is heated of heat exchanger, the fluid outlet connection rich oil outlet pipeline that is heated of heat exchanger, the other end of rich oil outlet pipeline is connected to on the debenzolization tower, be provided with temperature sensor on the rich oil outlet pipeline, the superheated steam pipeline of heat transfer fluid access connection of heat exchanger, the other end and the steam boiler of superheated steam pipeline are connected, the heat transfer fluid exit linkage condensate pipeline of heat exchanger, the other end of condensate pipeline is connected to on the low pressure flash tank.
In the above scheme, still parallelly connected be provided with debenzolization tower heat supply pipeline and regenerator heat supply pipeline on the superheated steam pipeline, debenzolization tower heat supply pipeline is connected with the debenzolization tower, and regenerator heat supply pipeline is connected with the regenerator, is provided with temperature sensor on debenzolization tower and the regenerator respectively.
In the scheme, a pressure reducing device is arranged on the rear section of a connector of the superheated steam pipeline and the steam boiler, a first adjusting device is arranged on the superheated steam pipeline and the front section of the connector of the heat exchanger, the first adjusting device is formed by sequentially connecting a stop valve, an electric adjusting valve and the stop valve in series, the electric adjusting valve is connected with a temperature sensor on the rich oil outlet pipeline through a lead, and the pressure reducing device is formed by sequentially connecting the stop valve, a pressure reducing valve and the stop valve in series.
In the above scheme, a bypass pipeline connected with the first adjusting device in parallel is arranged beside the first adjusting device, and a stop valve is arranged on the bypass pipeline.
In the scheme, the condensed water drainage device is arranged on the condensed water pipeline and is sequentially connected in series with the stop valve, the lever floating ball drainage valve and the stop valve, the bypass pipeline is connected beside the condensed water drainage device in parallel, and the stop valve is arranged on the bypass pipeline.
In the scheme, be provided with second adjusting device on the heat supply pipeline of debenzolization tower, second adjusting device is established ties by stop valve, electrical control valve, the three order of stop valve, electrical control valve on the second adjusting device passes through the wire with the temperature sensor on the debenzolization tower and is connected, be provided with decompression adjusting device on the regenerator heat supply pipeline, decompression adjusting device is established ties by four orders of stop valve, relief pressure valve, electrical control valve, stop valve, last electrical control valve of decompression adjusting device passes through the wire with the temperature sensor on the regenerator and is connected.
In the above scheme, the heat exchanger is a shell-and-tube heat exchanger.
In the above scheme, the rich oil inlet pipeline and the rich oil outlet pipeline are both provided with stop valves.
In the above scheme, low pressure steam pipeline is connected to low pressure flash tank upper end, and soft water pipeline is connected to low pressure flash tank lower extreme, is provided with water pump and boiler soft water tank on the soft water pipeline.
The utility model relates to a rich oil debenzolization heating system compares with prior art, and its beneficial effect is:
1. the system adopts the heat exchanger to heat the rich oil, no smoke is discharged, no sulfur or nitrogen oxide is generated, the pollution of the sulfur and the nitrogen oxide to the environment is reduced, and the cost for treating the sulfur and the nitrogen oxide is saved.
2. The system adopts the heat exchanger to heat the rich oil, does not burn coal gas, saves the operation cost and improves the economic benefit.
The flow rate is 280m3Economic benefit comparison table for tube furnace and rich oil heat exchanger
| Device | Medium | Gas consumption | Annual consumption | Unit price of | Amount (Wanyuan) | Remarks for note |
| Tubular heating furnace | Gas (es) | 2400m3/h | 2104.4 cubic meter | 0.5 yuan/m3 | 1052.2 | |
| Oil-rich heater | Steam generating device | 11t/h | 9.64 million tons | 75 yuan/t | 723.0 | |
| Saving cost | 329.2 |
3. The system adopts the heat exchanger to heat the rich oil, gas is not combusted, the danger of inflammable and explosive gas in the working process is avoided, and the safety performance of the system is greatly improved.
4. The heat exchanger is smaller than the tubular furnace, and the occupied area is greatly reduced, so that the occupied area is saved.
5. The tube furnace system is complicated, the equipment cost is higher, and compared with the heat exchanger and the tube furnace under the same condition, the equipment cost is lower.
Drawings
Fig. 1 is a schematic diagram of the heating system for rich oil debenzolization of the utility model.
In the figure:
-an electric control valve for controlling the flow of gas,
-a shut-off valve, which is,
-a lever floating ball drain valve,
-a water pump, which is connected to the pump,
-a temperature sensor for measuring the temperature of the fluid,
the system comprises a pressure reducing valve, a debenzolization tower, 2 leads, 3 second regulating devices, 4 debenzolization tower heat supply pipelines, 5 regenerator heat supply pipelines, 6 pressure reducing regulating devices, 7 regenerators, 8 steam boilers, 9 pressure reducing devices, 10 superheated steam pipelines, 11 first regulating devices, 12 bypass pipelines, 13 rich oil outlet pipelines, 14 shell-and-tube heat exchangers, 15 rich oil inlet pipelines, 16 condensed water pipelines, 17 condensed water draining devices, 18 low-pressure steam pipelines, 19 low-pressure flash tanks, 20 soft water pipelines, 21 water pumps, 22 boiler soft water tanks, 23 leads, 24 leads and 25 bypass pipelines.
Detailed Description
The utility model discloses a rich oil debenzolization heating system is described with specific example below with the accompanying drawing:
fig. 1 is a schematic diagram of the heating system for rich oil debenzolization of the utility model. In the figure, the rich oil debenzolization heating system comprises a shell-and-tube heat exchanger 14, a heated fluid inlet of the shell-and-tube heat exchanger 14 is connected with a rich oil inlet pipeline 15, a stop valve is arranged on the rich oil inlet pipeline 15, a heated fluid outlet of the shell-and-tube heat exchanger 14 is connected with a rich oil outlet pipeline 13, the upper end of the rich oil outlet pipeline 13 is connected to a debenzolization tower 1, a temperature sensor is arranged on the rich oil outlet pipeline 13, the stop valve is also arranged, a heat transfer fluid inlet of the shell-and-tube heat exchanger 14 is connected with an overheated steam pipeline 10, the right end of the overheated steam pipeline 10 is connected with a steam boiler 8, a heat transfer fluid outlet of the shell-and-tube heat exchanger 14 is connected with a condensed water pipeline 16, the right end of the condensed water pipeline 16 is connected to a low-pressure flash tank 19, the upper end of the low-pressure flash tank 19 is connected with a low-pressure steam pipeline 18, low-pressure steam is transported to other places through the pipeline for secondary utilization, the lower end of the low-pressure flash tank 19 is connected with a soft water pipeline 20, the soft water pipeline 20 is provided with a water pump 21 and a boiler soft water tank 22, and soft water from the boiler soft water tank 22 can be conveyed into the steam boiler 8 for reuse. The superheated steam pipeline 10 is also provided with a debenzolization tower heat supply pipeline 4 and a regenerator heat supply pipeline 5 in parallel, the debenzolization tower heat supply pipeline 4 is connected with the debenzolization tower 1, the regenerator heat supply pipeline 5 is connected with the regenerator 7, and the debenzolization tower 1 and the regenerator 7 are respectively provided with a temperature sensor. A pressure reducing device 9 is arranged on the rear section of a connector of the superheated steam pipeline 10 and the steam boiler, a first adjusting device 11 is arranged on the superheated steam pipeline 10 and the front section of the connector of the shell-and-tube heat exchanger 14, the first adjusting device 11 is formed by sequentially connecting a stop valve, an electric adjusting valve and the stop valve in series, the electric adjusting valve is connected with a temperature sensor on the rich oil outlet pipeline through a wire 2, and the electric adjusting valve adjusts the steam flow entering the heat exchanger according to the temperature transmitted by the temperature sensor. The pressure reducing device 9 is formed by sequentially connecting a stop valve, a pressure reducing valve and a stop valve in series. A bypass pipeline 12 connected with the first adjusting device in parallel is arranged beside the first adjusting device 11, and a stop valve is arranged on the bypass pipeline 12. The condensed water drainage device 17 is arranged on the condensed water pipeline 16, the condensed water drainage device 17 is sequentially connected in series by a stop valve, a lever floating ball drain valve and a stop valve, a bypass pipeline 25 is connected in parallel beside the condensed water drainage device 17, and the stop valve is arranged on the bypass pipeline 25 and used for pipeline maintenance.
Be provided with second adjusting device 3 on debenzolization tower heat supply pipeline 4, second adjusting device 3 is by the stop valve, electrical control valve, the three order series connection of stop valve, electrical control valve on the second adjusting device 3 passes through wire 23 with the temperature sensor on the debenzolization tower and is connected, be provided with decompression adjusting device 6 on regenerator heat supply pipeline 5, decompression adjusting device 6 is by the stop valve, the relief pressure valve, electrical control valve, four order series connections of stop valve, electrical control valve on the decompression adjusting device 6 passes through wire 24 with the temperature sensor on the regenerator and is connected.
The superheated steam pressure in the steam boiler 8 is 3.82MPa, the temperature is 350-400 ℃, the superheated steam pressure is reduced to 1.6MPa through the pressure reducing device 9, the pressure is fed into the shell-and-tube heat exchanger 14 to heat the rich oil, the steam flows through the shell side, the rich oil flows through the tube side, the temperature of the heated rich oil is about 180 ℃, and the heated rich oil enters the debenzolization tower 1 to be debenzolized.
The steam pipeline is divided into three paths, wherein the first path is that a superheated steam pipeline 10 is introduced into a heat exchanger to heat rich oil, the second path is that a heat supply pipeline 4 of the debenzolization tower is introduced into the debenzolization tower to be used as a standby heat source of the debenzolization tower, and the third path is that a heat supply pipeline 5 of the regenerator enters the regenerator to ensure the stable working condition of the regenerator. Condensed water generated by the heat exchanger enters a low-pressure flash tank 19 through a lever floating ball steam trap 17 to be subjected to steam-water separation, low-pressure steam and condensed water are generated through separation, the low-pressure steam enters a low-pressure steam pipe network of a chemical plant through a low-pressure steam pipeline 18 to be reused, and the condensed water returns to the steam boiler 8 through a boiler soft water tank 22 to be continuously used.
The heating system has the advantages of small occupied area, safety, environmental protection, no generation of gases such as sulfur, nitrogen oxides and the like, no danger of burning coal gas, cost saving and economic benefit improvement.
The above description is only a preferred embodiment of the present invention, and the present invention is not limited to the above description, and although the present invention has been disclosed with reference to the preferred embodiment, it is not limited to the present invention, and any skilled person in the art can make various changes or modifications equivalent to the above embodiments without departing from the scope of the present invention, but all the modifications, changes and modifications of the above embodiments by the technical spirit of the present invention are within the scope of the present invention.
Claims (9)
1. A rich oil debenzolization heating system which characterized in that: the heat exchanger comprises a heat exchanger, the fluid inlet connection rich oil inlet pipeline that is heated of heat exchanger, the fluid outlet connection rich oil outlet pipeline that is heated of heat exchanger, the other end of rich oil outlet pipeline is connected to the debenzolization tower on, be provided with temperature sensor on the rich oil outlet pipeline, the superheated steam pipeline of heat transfer fluid access connection of heat exchanger, the other end and the steam boiler of superheated steam pipeline are connected, the heat transfer fluid exit linkage condensate pipe of heat exchanger, the other end of condensate pipe is connected to on the low pressure flash tank.
2. The heating system for oil-rich debenzolization as claimed in claim 1, wherein: the superheated steam pipeline is also provided with a debenzolization tower heat supply pipeline and a regenerator heat supply pipeline in parallel, the debenzolization tower heat supply pipeline is connected with the debenzolization tower, the regenerator heat supply pipeline is connected with the regenerator, and the debenzolization tower and the regenerator are respectively provided with a temperature sensor.
3. The heating system for oil-rich debenzolization as claimed in claim 1, wherein: the superheated steam pipeline is provided with a pressure reducing device at the rear section of a connector of the steam boiler, the superheated steam pipeline is provided with a first adjusting device at the front section of the connector of the heat exchanger, the first adjusting device is sequentially connected in series with a stop valve, an electric adjusting valve and a stop valve, the electric adjusting valve is connected with a temperature sensor on the rich oil outlet pipeline through a lead, and the pressure reducing device is sequentially connected in series with the stop valve, a pressure reducing valve and the stop valve.
4. The heating system for oil-rich debenzolization as claimed in claim 3, wherein: and a bypass pipeline connected with the first adjusting device in parallel is arranged beside the first adjusting device, and a stop valve is arranged on the bypass pipeline.
5. The heating system for oil-rich debenzolization as claimed in claim 1, wherein: the condensed water drainage device is formed by sequentially connecting a stop valve, a lever floating ball drain valve and the stop valve in series, a bypass pipeline is connected beside the condensed water drainage device in parallel, and the stop valve is arranged on the bypass pipeline.
6. The heating system for oil-rich debenzolization as claimed in claim 2, wherein: be provided with second adjusting device on the heat supply pipeline of debenzolization tower, second adjusting device is established ties by stop valve, electrical control valve, the three order of stop valve, electrical control valve on the second adjusting device passes through the wire with the temperature sensor on the debenzolization tower and is connected, be provided with decompression adjusting device on the regenerator heat supply pipeline, decompression adjusting device is established ties by four orders of stop valve, relief pressure valve, electrical control valve, stop valve, last electrical control valve of decompression adjusting device passes through the wire with the temperature sensor on the regenerator and is connected.
7. The heating system for oil-rich debenzolization as claimed in claim 1, wherein: the heat exchanger is a shell-and-tube heat exchanger.
8. The heating system for oil-rich debenzolization as claimed in claim 1, wherein: and the rich oil inlet pipeline and the rich oil outlet pipeline are both provided with stop valves.
9. The heating system for oil-rich debenzolization as claimed in claim 1, wherein: the low-pressure steam pipeline is connected to low pressure flash tank upper end, and soft water pipeline is connected to the low pressure flash tank lower extreme, is provided with water pump and boiler soft water groove on the soft water pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022558723.7U CN213977550U (en) | 2020-11-06 | 2020-11-06 | Rich oil debenzolization heating system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022558723.7U CN213977550U (en) | 2020-11-06 | 2020-11-06 | Rich oil debenzolization heating system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213977550U true CN213977550U (en) | 2021-08-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022558723.7U Expired - Fee Related CN213977550U (en) | 2020-11-06 | 2020-11-06 | Rich oil debenzolization heating system |
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| Country | Link |
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| CN (1) | CN213977550U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112280587A (en) * | 2020-11-06 | 2021-01-29 | 陕西紫兆装备制造有限公司 | Rich oil debenzolization heating system |
-
2020
- 2020-11-06 CN CN202022558723.7U patent/CN213977550U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112280587A (en) * | 2020-11-06 | 2021-01-29 | 陕西紫兆装备制造有限公司 | Rich oil debenzolization heating system |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20210817 Termination date: 20211106 |
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| CF01 | Termination of patent right due to non-payment of annual fee |