CN220867337U - Light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment - Google Patents
Light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment Download PDFInfo
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- CN220867337U CN220867337U CN202322609162.2U CN202322609162U CN220867337U CN 220867337 U CN220867337 U CN 220867337U CN 202322609162 U CN202322609162 U CN 202322609162U CN 220867337 U CN220867337 U CN 220867337U
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- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 62
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 62
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 62
- 238000000197 pyrolysis Methods 0.000 title claims description 18
- 238000005336 cracking Methods 0.000 claims abstract description 74
- 238000000034 method Methods 0.000 claims abstract description 32
- 238000010790 dilution Methods 0.000 claims abstract description 30
- 239000012895 dilution Substances 0.000 claims abstract description 30
- 230000008569 process Effects 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 15
- 238000000926 separation method Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000003546 flue gas Substances 0.000 claims abstract description 10
- 239000000446 fuel Substances 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000001816 cooling Methods 0.000 claims description 8
- 230000009467 reduction Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 abstract description 6
- 239000000126 substance Substances 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 15
- 230000005855 radiation Effects 0.000 description 7
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 6
- 239000005977 Ethylene Substances 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000010926 purge Methods 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a light hydrocarbon cracking furnace temperature-raising and energy-saving device, which belongs to the technical field of chemical equipment and comprises a light hydrocarbon cracking furnace and the like, wherein a combustor, an internal pipeline a and an internal pipeline b are arranged in the light hydrocarbon cracking furnace, the combustor is communicated with a fuel pipeline, the top of the light hydrocarbon cracking furnace is communicated with an induced draft fan through a pipeline, the induced draft fan is communicated with a flue gas outlet pipeline, a feeding pipeline is communicated with the internal pipeline a, the internal pipeline a is communicated with an internal pipeline b through a pipeline, the internal pipeline b is communicated with a cooler b through a pipeline, the coolers b are respectively communicated with a discharging pipeline, a process water feeding pipeline is communicated with a dilution steam generator, the dilution steam generator is communicated with the feeding pipeline, and a burnt air compressor is further arranged, the burnt air compressor is communicated with a filtered air inlet pipeline, the burnt air compressor is communicated with a gas-liquid separation tank through a pipeline, and the gas-liquid separation tank is communicated with a feeding pipeline through a pipeline. The control method for the temperature rise and fall process of the light hydrocarbon cracking furnace has the advantages of safety, effectiveness, energy conservation and the like.
Description
Technical Field
The utility model belongs to the technical field of chemical production, and particularly relates to temperature-raising and energy-saving equipment for a light hydrocarbon cracking furnace.
Background
Ethylene is used as a tap in the chemical industry, and its yield directly determines the industrial development level of a country. In recent years, various ethylene production apparatuses have been continuously constructed, and it is an important task to reduce the energy consumption of the apparatus in order to make the apparatus viable for a long time in a large number of apparatuses. Therefore, in each large ethylene plant, it is important to find a way to reduce the energy consumption of the plant through a series of technological reforms.
With the gradual maturity of the process for preparing ethylene by cracking light hydrocarbon, the traditional naphtha cracking and MTO process is continuously faced with the examination. The light hydrocarbon cracking process has advantages from the process itself because of lower single-pass energy consumption and higher yield compared with the two processes. However, along with continuous fluctuation of crude oil price, the raw material cost of the naphtha cracking process is continuously reduced, so that the device cost is continuously reduced, and great competitiveness is brought to the device. In order to ensure that the advantages of light hydrocarbon cracking can exist for a long time, relevant technicians of each device of the light hydrocarbon cracking process continuously study, reform and perfect the existing process, and strive for the existing process to be more energy-saving and thus more competitive.
The light hydrocarbon cracking furnace is used as one of the core devices of the ethylene preparation device by light hydrocarbon cracking, and the long-period operation, energy saving, consumption reduction and emission reduction of the devices greatly influence the comprehensive operation cost of the device. The main raw materials of domestic ethylene devices are naphtha, straight-run diesel oil and the like, and along with development of shale gas and oilfield associated gas in recent years, the light hydrocarbon cracking process is widely applied. Because the operation of the cracking furnace needs periodic burning and overhauling, a great deal of steam and fuel are lost in the processes, and how to reduce the consumption in the processes becomes one of key factors for optimizing the device.
Disclosure of Invention
In order to solve the energy consumption problem of the existing device, the main purpose of the utility model is to provide a safe, effective and energy-saving system for saving steam consumption in the process of heating and cooling a light hydrocarbon cracking furnace and an application method thereof.
The utility model provides a light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment, including light hydrocarbon pyrolysis furnace, the draught fan, dilute steam generator, cooler a, the feed line, process water feed line and cooler b, be equipped with combustor and interior pipeline a and interior pipeline b in the light hydrocarbon pyrolysis furnace, the combustor is linked together with the fuel pipe line, the top of light hydrocarbon pyrolysis furnace is linked together with the draught fan through the pipeline, the draught fan is linked together with the flue gas export pipeline, feed line is linked together with interior pipeline a, interior pipeline a is linked together with interior pipeline b through the pipeline, interior pipeline b is linked together with cooler b through the pipeline, cooler b is linked together with the discharging pipeline respectively, process water feed line is linked together with dilute steam generator, dilute steam generator is linked together with the feed line, above-mentioned structure belongs to current structure, the applicant is not repeated here.
The utility model has the core improvement that the device is also provided with a charring air compressor which is communicated with a filtered air inlet pipeline, the charring air compressor is communicated with a gas-liquid separation tank through a pipeline, and the gas-liquid separation tank is communicated with a feed pipeline through a pipeline.
Preferably: in order to achieve better energy-saving effect, the cooler b is communicated with a burnt air return pipeline which is communicated with the bottom of the light hydrocarbon cracking furnace.
The working principle of the utility model is as follows: two paths of materials enter in the heating and cooling process of the light hydrocarbon cracking furnace, and filtered air is boosted and cooled by a burnt air compressor and then enters the light hydrocarbon cracking furnace by controlling the flow rate by a regulating valve; the process water generates dilution steam through a dilution steam generator, the flow is controlled through a regulating valve, and the dilution steam and the burnt air are mixed and then enter a light hydrocarbon cracking furnace together; the air and steam mixture at the outlet of the light hydrocarbon cracking furnace is discharged to the hearth of the cracking furnace, and the heat is recovered through the convection section and then is discharged to the atmosphere as the flue gas of the cracking furnace.
The light hydrocarbon cracking furnace comprises a feeding pipeline, a discharging pipeline, a medium inlet and a medium outlet, wherein the material feeding pipeline is connected with the gas outlets of the scorching air and dilution steam generator, and the material discharging pipeline is connected with the cooler b; the dilution steam material is superheated steam provided by the dilution steam generator, and the charred air medium is high-temperature gas discharged from an air outlet at the top of the charred air compressor outlet liquid separating tank.
The light hydrocarbon cracking furnace comprises a radiation chamber and a convection section, the top of the radiation chamber is connected with an induced draft fan, the dilution steam generator is connected with a process water feeding pipeline, process water is heated and gasified after contacting with high-pressure steam in the dilution steam generator, so that dilution steam is generated, and the dilution steam is sent to the cracking furnace.
Heating a light hydrocarbon cracking furnace: after the light hydrocarbon cracking furnace is ignited and begins to heat, the burnt air output by the burnt air compressor is introduced into the light hydrocarbon cracking furnace for furnace tube purging through the cooler a and the gas-liquid separation tank under flow indication control; in the heating process, diluent steam at the outlet of the diluent steam generator is subjected to flow indication control, mixed with burnt air and then introduced into a cracking furnace to be used as furnace tube protection gas; cooling the gas blown out from the outlet of the light hydrocarbon cracking furnace, delivering the cooled gas to the hearth of the radiation chamber of the cracking furnace, recovering heat, and discharging the recovered heat into the atmosphere as flue gas by an induced draft fan; and (3) stopping feeding of scorching air along with the increase of the temperature of the cracking furnace to the hot standby temperature of 820 ℃ at the speed of 100 ℃/h, and improving the flow of dilution steam to prepare blind plate dropping and feeding.
Cooling the cracking furnace: after the pyrolysis furnace is burnt, the flow of the burnt air output by the burnt air compressor is kept unchanged, the outlet temperature of the pyrolysis furnace is reduced at the speed of 100 ℃ per hour along with the temperature of the light hydrocarbon pyrolysis furnace, and the flow of dilution steam sent to the pyrolysis furnace by the dilution steam generator is gradually reduced; diluting mixed gas of steam and burnt air, cooling the gas blown out from an outlet of a light hydrocarbon cracking furnace, delivering the cooled gas to a hearth of a radiation chamber of the cracking furnace, recovering heat, and discharging the recovered heat into the atmosphere as flue gas through an induced draft fan; and (3) reducing the temperature of the light hydrocarbon cracking furnace to 200 ℃, stopping introducing dilution steam, reducing the temperature of the light hydrocarbon cracking furnace to 100 ℃, stopping introducing scorching air, and preparing for flameout of the light hydrocarbon cracking furnace and falling of the blind plate.
The temperature of dilution steam after the dilution steam generator is overheated is 175-185 ℃; the temperature of the scorching air generated by the scorching air compressor is 120-140 ℃; after passing through the cooler a and the gas-liquid separation tank, the temperature of the burnt air blown out from the top air outlet is 40-50 ℃.
The temperature of the dilution steam which is introduced into the cracking furnace is 175-185 ℃ and the pressure is 0.6-0.7 MPa; the temperature of the burnt air is 40-50 ℃ and the pressure is 0.6-0.7 MPa.
Compared with the prior art, the utility model has the following advantages:
1) The method has the advantages that the burnt air is introduced when the cracking furnace is ignited and heated, and residual impurities and moisture in the furnace tube of the cracking furnace are blown out in a purging mode, so that coking and blocking of the furnace tube can be prevented, the service life of the furnace tube and the operation period of the cracking furnace are influenced, and even potential safety hazards caused by furnace tube breakage occur in the feeding process;
2) The burnt air is continuously introduced in the heating and cooling processes of the cracking furnace, so that the furnace tube temperature can be protected by replacing a part of steam, the consumption of diluted steam can be reduced, the load of a diluted steam generator can be greatly reduced, the consumption of heating steam required by the generator is saved, and meanwhile, the requirement on process water is reduced;
3) In the process of heating the cracking furnace to the hot standby temperature, the furnace tube can be burned again in the heating period due to the continuous feeding of the burning air, so that the residual impurities and the coke layer in the furnace tube are thoroughly removed, the running period of the cracking furnace can be effectively prolonged, and the running safety and stability of the cracking furnace are improved.
Drawings
Fig. 1 is a schematic structural diagram of the working principle of the utility model.
Wherein, 1-light hydrocarbon cracking furnace; 2-induced draft fan; 3-dilution steam generator; 4-a burnt air compressor; 5-a char air cooler; 6-a gas-liquid separation tank; 7-a feed line; 8-a process water feed line; 9-filtered air inlet line; 10-cooler a; 11-a discharge line; 12-an internal line b; 13-char air return line; 14-a radiation chamber of the cracking furnace; 15-a convection section of the cracking furnace; 16-a flue gas outlet line; 17-a fuel line; 18-a burner; 19-internal line a.
Detailed Description
The utility model is further illustrated by the following specific examples. These examples are merely illustrative of the utility model and are not intended to limit the scope of the utility model.
Example 1
As shown in figure 1 of the drawings,
The utility model provides a light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment, including light hydrocarbon pyrolysis furnace 1, induced draught fan 2, dilute steam generator 3, cooler a5, feed line 7, process water feed line 8 and cooler b10, be equipped with combustor 18 and internal line a19 and internal line b12 in the light hydrocarbon pyrolysis furnace 1, combustor 18 is linked together with fuel line 17, the top of light hydrocarbon pyrolysis furnace 1 is linked together through the pipeline with induced draught fan 2, induced draught fan 2 is linked together with flue gas outlet line 16, feed line 7 is linked together with internal line a19, internal line a19 is linked together through the pipeline with internal line b12, internal line b12 is linked together with cooler b10 through the pipeline, cooler b10 is linked together with discharge line 11 respectively, process water feed line 8 is linked together with dilute steam generator 3, dilute steam generator 3 is linked together with feed line 7, characterized in that still is equipped with burnt air compressor 4, burnt air compressor 4 is linked together with filtered air admission line 9, burnt air compressor 4 is linked together with gas-liquid separator 6 through the pipeline, gas-liquid separator tank 6 is linked together through pipeline 7. The cooler b10 is communicated with a burnt air return pipeline 13, and the burnt air return pipeline 13 is communicated with the bottom of the light hydrocarbon cracking furnace 1.
Heating a light hydrocarbon cracking furnace: after the light hydrocarbon cracking furnace 1 is ignited and begins to heat, the burnt air output by the burnt air compressor 4 is introduced into the light hydrocarbon cracking furnace for furnace tube purging through the cooler a5 and the gas-liquid separation tank 6 under flow indication control; in the heating process, the diluted steam at the outlet of the diluted steam generator 3 is mixed with the burnt air and then is introduced into a light hydrocarbon cracking furnace to be used as furnace tube protecting gas after flow indication control; the gas blown out from the outlet of the light hydrocarbon cracking furnace is cooled by a cooler b10 and then is sent to a hearth 14 of a radiation chamber of the cracking furnace, and after heat is recovered, the gas is taken as flue gas to be discharged into the atmosphere by an induced draft fan 2; and (3) stopping feeding of scorching air along with the increase of the temperature of the cracking furnace to the hot standby temperature of 820 ℃ at the speed of 100 ℃/h, and improving the flow of dilution steam to prepare blind plate dropping and feeding.
Cooling the light hydrocarbon cracking furnace: after the light hydrocarbon cracking furnace 1 is burnt, the burnt air output by the burnt air compressor 4 is kept constant in flow, and the flow of dilution steam sent to the light hydrocarbon cracking furnace by the dilution steam generator 3 is gradually reduced along with the reduction of the furnace outlet temperature at the speed of 100 ℃/h; the mixed gas of the dilution steam and the burnt air is cooled 10 and then sent to a hearth 14 of a radiation chamber of the cracking furnace, and after heat is recovered, the mixed gas is discharged into the atmosphere as flue gas through a draught fan 2; and the temperature of the cracking furnace is reduced to 200 ℃, the dilution steam is stopped from being introduced, the temperature of the cracking furnace is reduced to 100 ℃, the introduction of the scorching air is stopped, and the flameout of the cracking furnace and the falling of the blind plate are prepared.
The temperature of the dilution steam after being overheated by the dilution steam generator 3 is 175-185 ℃; the temperature of the burnt air generated by the burnt air compressor 4 is 120-140 ℃; after passing through the cooler a5 and the gas-liquid separation tank 6, the temperature of the burnt air blown out from the top air outlet is 40-50 ℃.
The diluted steam is introduced into the light hydrocarbon cracking furnace 1 at the temperature of 175-185 ℃ and the pressure of 0.6-0.7 MPa; the temperature of the burnt air which is introduced into the light hydrocarbon cracking furnace 1 is 40-50 ℃ and the pressure is 0.6-0.7 MPa.
The above embodiments are only for illustrating the present utility model, not for limiting the present utility model, and various changes and modifications may be made by one of ordinary skill in the relevant art without departing from the spirit and scope of the present utility model, and therefore, all equivalent technical solutions are also within the scope of the present utility model, and the scope of the present utility model is defined by the claims.
Claims (4)
1. The utility model provides a light hydrocarbon pyrolysis furnace temperature rise and reduction energy-saving equipment, including light hydrocarbon pyrolysis furnace (1), draught fan (2), dilute steam generator (3), cooler a (5), feed line (7), process water feed line (8) and cooler b (10), be equipped with combustor (18) and inside pipeline a (19) and inside pipeline b (12) in light hydrocarbon pyrolysis furnace (1), combustor (18) are linked together with fuel line (17), the top of light hydrocarbon pyrolysis furnace (1) is linked together with draught fan (2) through the pipeline, draught fan (2) is linked together with flue gas outlet pipeline (16), feed line (7) are linked together with inside pipeline a (19), inside pipeline a (19) are linked together with inside pipeline b (12) through the pipeline, inside pipeline b (12) are linked together with cooler b (10) through the pipeline, cooler b (10) are linked together with ejection of compact pipeline (11) respectively, process water feed line (8) are linked together with dilute steam generator (3), dilute steam generator (3) are linked together with feed line (7) characterized in that,
The device is also provided with a burning air compressor (4), the burning air compressor (4) is communicated with a filtered air inlet pipeline (9), the burning air compressor (4) is communicated with a gas-liquid separation tank (6) through a pipeline, and the gas-liquid separation tank (6) is communicated with a feeding pipeline (7) through a pipeline.
2. The light hydrocarbon cracking furnace temperature-increasing and energy-saving equipment according to claim 1, wherein the cooler b (10) is communicated with a burnt air return line (13), and the burnt air return line (13) is communicated with the bottom of the light hydrocarbon cracking furnace (1).
3. The light hydrocarbon cracking furnace temperature-increasing and energy-saving equipment according to claim 1, which is characterized in that the temperature of dilution steam after being overheated by the dilution steam generator (3) is 175-185 ℃; the temperature of the burnt air generated by the burnt air compressor 4 is 120-140 ℃; after passing through the cooler a (5) and the gas-liquid separation tank (6), the temperature of the burnt air blown out from the top air outlet is 40-50 ℃.
4. The energy-saving equipment for heating and cooling the light hydrocarbon cracking furnace according to claim 1, wherein the temperature of the dilution steam fed into the light hydrocarbon cracking furnace (1) is 175-185 ℃ and the pressure is 0.6-0.7 MPa; the temperature of the burnt air which is introduced into the light hydrocarbon cracking furnace (1) is 40-50 ℃ and the pressure is 0.6-0.7 MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322609162.2U CN220867337U (en) | 2023-09-26 | 2023-09-26 | Light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322609162.2U CN220867337U (en) | 2023-09-26 | 2023-09-26 | Light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220867337U true CN220867337U (en) | 2024-04-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322609162.2U Active CN220867337U (en) | 2023-09-26 | 2023-09-26 | Light hydrocarbon pyrolysis furnace temperature rise and fall energy-saving equipment |
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| Country | Link |
|---|---|
| CN (1) | CN220867337U (en) |
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- 2023-09-26 CN CN202322609162.2U patent/CN220867337U/en active Active
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