CN210462963U - Dilute steam generator capable of controlling steam/hydrocarbon ratio for light hydrocarbon thermal cracking - Google Patents
Dilute steam generator capable of controlling steam/hydrocarbon ratio for light hydrocarbon thermal cracking Download PDFInfo
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- CN210462963U CN210462963U CN201921431464.2U CN201921431464U CN210462963U CN 210462963 U CN210462963 U CN 210462963U CN 201921431464 U CN201921431464 U CN 201921431464U CN 210462963 U CN210462963 U CN 210462963U
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Abstract
The utility model discloses a diluted steam generating device for light hydrocarbon thermal cracking, which can control the steam/hydrocarbon ratio and mainly comprises a light hydrocarbon feeding saturation tower, a process water circulating pump, a circulating heater, a saturated feeding superheater and a sewage cooler; one side of the lower part of the light hydrocarbon feeding saturation tower is communicated with a light hydrocarbon feeding pipeline, the other side of the lower part of the light hydrocarbon feeding saturation tower is provided with a process water inlet, and the process water inlet is communicated with a process water inlet pipeline; the bottom of the light hydrocarbon feeding saturation tower is provided with a process water extraction port which is sequentially communicated with a process water circulating pump, a circulating heater and a process water inlet through pipelines; a sewage discharge outlet is arranged at the bottom of the light hydrocarbon feeding saturated tower and is communicated with a sewage discharge cooler, and the sewage discharge cooler is connected to a sewage treatment system; the top of light hydrocarbon feeding saturation tower sets up the export, and the export links to each other with saturated feeding over heater, and saturated feeding over heater is connected to the pyrolysis furnace. The utility model integrates the functions of steam dilution and steam/hydrocarbon ratio control, and has simple operation and reduced operation cost.
Description
Technical Field
The utility model relates to a light hydrocarbon thermal cracking of steerable steam hydrocarbon ratio is with diluting steam generator belongs to the chemical industry equipment field.
Background
At present, the ethylene plant in the world is mainly used for petroleum hydrocarbon steam thermal cracking, namely, raw materials such as light hydrocarbon, naphtha and straight-run diesel oil are mixed with dilution steam according to a certain proportion, cracking reaction is carried out at high temperature, and chemical basic raw materials such as ethylene, propylene and the like are generated through cooling, compression, rectification separation and the like. The injection of dilution steam into the ethylene device can reduce the hydrocarbon partial pressure of the radiation furnace tube of the cracking furnace, improve the selectivity of main products such as ethylene, propylene and the like, stabilize the temperature of the furnace tube and inhibit the coking of the furnace tube. Generally, the cracking feedstock of an ethylene plant is ethane, propane, butane, naphtha, light diesel, hydrocracked distillate oil, etc., and generally the lighter the feedstock, the higher the ethylene yield of the plant, and the lower the investment and energy consumption.
The main raw materials of the domestic ethylene device are naphtha, straight-run diesel oil and the like, the cracking product contains a large amount of heavy fractions such as gasoline, diesel oil and fuel oil and the like, the heavy fractions are easy to mix with water and are difficult to separate oil from water due to emulsification, so a quenching oil tower and a quenching water tower are arranged in a quenching area, a dilution steam generation system takes quenching oil as a heat source, dilution steam is generated by recovering heat of the quenching oil, and meanwhile, medium-pressure steam is used as the heat source to generate dilution steam for later use. With the development of shale gas and oil field associated gas, the light hydrocarbon cracking process is widely applied. The cracking products of light hydrocarbon mainly comprise light components below C4s, heavy fractions such as gasoline, diesel oil and fuel oil are few, and circulation cannot be established in a quenching oil tower, so that equipment investment waste is caused, sufficient dilution steam cannot be generated by taking the quenching oil as a heat source, and the energy consumption of the dilution steam generated by taking medium-pressure steam as the heat source is high, so that the dilution steam generating system of the traditional ethylene device is not suitable for a light hydrocarbon thermal cracking device.
Disclosure of Invention
For solving the problem that present ethylene device dilutes steam generation system and is not suitable for light hydrocarbon thermal cracking to take place to dilute steam, the utility model provides a light hydrocarbon thermal cracking of steerable steam hydrocarbon ratio is with diluting steam generation device, this generating device collection dilutes steam generation and steam hydrocarbon ratio control in an organic whole, easy operation, and reducible medium pressure steam's use amount, reduction operating cost.
The utility model provides a technical scheme that technical problem adopted is: a dilution steam generating device for light hydrocarbon thermal cracking capable of controlling steam/hydrocarbon ratio, which mainly comprises a light hydrocarbon feeding saturation tower, a process water circulating pump, a circulating heater, a saturated feeding superheater and a blowdown cooler; one side of the lower part of the light hydrocarbon feeding saturation tower is communicated with a light hydrocarbon feeding pipeline, the other side of the lower part of the light hydrocarbon feeding saturation tower is provided with a process water inlet, and the process water inlet is communicated with a process water inlet pipeline; the bottom of the light hydrocarbon feeding saturation tower is provided with a process water extraction port, and the process water extraction port is sequentially communicated with a process water circulating pump, a circulating heater and a process water inlet arranged at the upper part of the light hydrocarbon feeding saturation tower through pipelines; the bottom of the light hydrocarbon feeding saturated tower is also provided with a drain outlet which is communicated with a blowdown cooler, and the blowdown cooler is connected to a sewage treatment system; the top of the light hydrocarbon feeding saturation tower is provided with an outlet, the outlet is connected with a saturated feeding superheater, and the saturated feeding superheater is connected to the cracking furnace.
Furthermore, a partition plate, a gas distributor, a packing area and a demister are sequentially arranged in the light hydrocarbon feeding saturation tower from bottom to top.
Furthermore, the process water inlet and the process water extraction opening are arranged on the same side of the light hydrocarbon feeding saturation tower, the partition plate is arranged at the bottom of the light hydrocarbon feeding saturation tower, and the process water inlet, the process water extraction opening and the sewage discharge opening are separated by the partition plate.
Furthermore, the cross section of the partition plate is L-shaped, and a gap is reserved between the partition plate and the bottom of the light hydrocarbon feeding saturation tower, so that the two sides of the partition plate are communicated.
Further, the gas distributor is arranged above the partition plate in the light hydrocarbon feeding saturation tower, and the light hydrocarbon feeding pipeline extends into the tower and then is connected to the gas distributor.
Further, the packing area is arranged above the gas distributor in the light hydrocarbon feeding saturation tower, and bulk packing or regular packing is arranged in the packing area.
Further, the demister is arranged above the packing area in the light hydrocarbon feeding saturation tower and is a stainless steel demister net.
Further, the process water inlet is arranged between the packing area and the demister.
Furthermore, an outlet at the top of the light hydrocarbon feeding saturation tower is connected with the saturated feeding superheater through a discharge pipeline, the discharge pipeline inclines towards the light hydrocarbon feeding saturation tower, and the inclination of the inclination is 1/500-1/100.
Further, the circulating heater and the saturated feeding superheater are heated by low-pressure steam.
The operation mode of the dilution steam generating device is as follows:
the superheated steam/light hydrocarbon mixture in the light hydrocarbon feeding saturation tower is cracked in the cracking furnace, the cracked gas cracked in the cracking furnace is quenched and further cooled in the quenching water tower, the diluted steam in the cracked gas is condensed into oil-containing quenching water, the oil-containing quenching water is purified, the separated process water enters the light hydrocarbon feeding saturation tower through the process water inlet pipeline and the process water inlet, and the process water flow is controlled to maintain the liquid level in the tower and is not higher than the gas distributor. The process water is pumped out from a process water pumping outlet through a process water circulating pump and sent into a circulating heater, and after being heated by low-pressure steam in the circulating heater, the process water enters a packing area from the upper part of a light hydrocarbon feeding saturation tower and flows downwards along the packing area.
Light hydrocarbon enters a light hydrocarbon feeding saturation tower from a light hydrocarbon feeding pipeline after being preheated by flue gas in a convection section of a cracking furnace, the light hydrocarbon flows upwards along the inside of the tower after being dispersed uniformly through a gas distributor, the light hydrocarbon is in countercurrent contact with circulating process water heated by low-pressure steam in a packing area, dilution steam is generated after the process water is vaporized, the dilution steam is saturated in the light hydrocarbon, partial pressure is provided by the preheated light hydrocarbon under the condition of certain total pressure, the vaporization temperature of the process water is reduced, and the energy consumption of a device is reduced. By controlling the flow rate and temperature of the recycled process water, the desired steam to hydrocarbon ratio is achieved.
The light hydrocarbon after water saturation removes water drops and impurities carried in the gas phase through a stainless steel defoaming net, and then enters a saturated feeding superheater to be superheated by low-pressure steam, so that the saturated steam in the steam/light hydrocarbon feeding mixture is prevented from being condensed on the pipe wall to form two-phase flow in the flowing process. The discharge pipeline between the outlet at the top of the light hydrocarbon feeding saturation tower and the saturated feeding superheater inclines towards the light hydrocarbon feeding saturation tower, so that condensate in the steam/light hydrocarbon feeding mixture returns to the light hydrocarbon feeding saturation tower. The bottom of the light hydrocarbon feeding saturation tower is provided with continuous blowdown to maintain the quality of the process water in the light hydrocarbon feeding saturation tower, and the process water is cooled by cooling water in the blowdown cooler and then sent to a boundary region sewage treatment system to remove dissolved solids and salts accumulated by vaporization of the process water.
The utility model has the advantages that: compared with the prior art, the utility model provides a dilute steam generator and accomplish in light hydrocarbon feeding saturation tower and dilute steam generation and steam/hydrocarbon ratio control, easy operation, and technology water and raw materials light hydrocarbon direct contact, technology water vaporization temperature is lower, can use low pressure steam as the heat source, has reduced the device energy consumption.
Drawings
Fig. 1 is a schematic structural diagram of the dilution steam generator provided by the present invention.
Fig. 2 is a process flow chart of the process water recycling of the dilution steam generating device provided by the present invention.
Wherein, 1-outlet; 2-stainless steel defoaming net; 3-a packing zone; 4-light hydrocarbon feeding saturation tower; a 5-light hydrocarbon feed conduit; 6-a separator; 7-a sewage draining outlet; 8-a process water inlet pipe; 9-blowdown cooler; 10-process water circulating pump; 11-a process water extraction port; 12-a process water inlet; 13-a gas distributor; 14-process water inlet; 15-a discharge pipeline; 16-saturated feed superheater; 17-a circulation heater; 18-a cracking furnace; 19-a quench water tower; 20-a process water treatment unit.
Detailed Description
The invention is further illustrated by the following specific examples. These examples are intended to illustrate the invention and are not intended to limit the scope of the invention.
Examples
As shown in fig. 1 and 2, a diluted steam generator for thermal cracking of light hydrocarbon with controllable steam/hydrocarbon ratio mainly comprises a light hydrocarbon feeding saturation tower 4, a process water circulating pump 10, a circulating heater 17, a saturated feeding superheater 16 and a blowdown cooler 9; one side of the lower part of the light hydrocarbon feeding saturation tower 4 is communicated with a light hydrocarbon feeding pipeline 5, the other side of the lower part of the light hydrocarbon feeding saturation tower 4 is provided with a process water inlet 12, and the process water inlet 12 is communicated with a process water inlet pipeline 8; the bottom of the light hydrocarbon feeding saturation tower 4 is provided with a process water extraction port 11, and the process water extraction port 11 is sequentially communicated with a process water circulating pump 10, a circulating heater 17 and a process water inlet 14 arranged at the upper part of the light hydrocarbon feeding saturation tower 4 through pipelines; the process water inlet 12 and the process water inlet 14 are on the same side of the light hydrocarbon feed saturation column 4. The bottom of the light hydrocarbon feeding saturation tower 4 is also provided with a sewage outlet 7, wherein the position of the sewage outlet 7 at the bottom and the position of the process water inlet 12 are in opposite directions on the light hydrocarbon feeding saturation tower 4; the sewage discharge outlet 7 is communicated with a sewage discharge cooler 9, and the sewage discharge cooler 9 is connected to a sewage treatment system; an outlet 1 is arranged at the top of the light hydrocarbon feeding saturation tower 4, the outlet 1 is connected with a saturated feeding superheater 16, and the saturated feeding superheater 16 is connected to a cracking furnace 18. The circulating heater 17 and the saturated feeding superheater 16 are heated by low-pressure steam.
And the light hydrocarbon feeding saturation tower 4 is internally provided with a partition plate 6, a gas distributor 13, a packing area 3 and a demister in sequence from bottom to top. The process water inlet 12 and the process water extraction port 11 are arranged on the same side of the light hydrocarbon feeding saturation tower 4, the partition plate 6 is arranged at the bottom of the light hydrocarbon feeding saturation tower 4, the cross section of the partition plate 6 is L-shaped, and a gap is formed between the partition plate 6 and the bottom of the light hydrocarbon feeding saturation tower 4, so that the two sides of the partition plate 6 are communicated. The process water inlet 12 and the process water outlet 11 are separated from the sewage outlet 7 by the partition plate 6; one side of the clapboard 6 is fresh process water, and the other side is residual water after vaporization.
The gas distributor 13 is arranged above the partition plate 6 in the light hydrocarbon feeding saturation tower 4, and the light hydrocarbon feeding pipeline 5 extends into the tower and then is connected to the gas distributor 13. The packing area 3 is arranged above the gas distributor 13 in the light hydrocarbon feeding saturation tower 4, and bulk packing or regular packing is arranged in the packing area 3. The demister is arranged above the packing area 3 in the light hydrocarbon feeding saturation tower 4 and is a stainless steel demister 2. The process water inlet 14 is provided between the packing section 3 and the demister. The top outlet 1 of the light hydrocarbon feeding saturation tower 4 is connected with the saturated feeding superheater 16 through a discharge pipeline 15, the discharge pipeline 15 inclines towards the light hydrocarbon feeding saturation tower 4, and the inclination of the inclination is 1/500-1/100.
The working method of the dilution steam generating device is as follows:
fresh light hydrocarbon is preheated to 160 ℃ in a convection section of the cracking furnace 18, enters the light hydrocarbon feeding saturation tower 4 through the light hydrocarbon feeding pipeline 5, is uniformly distributed by the gas distributor 13, flows upwards along the inside of the tower, and is in countercurrent contact with circulating process water heated by low-pressure steam on the surface of the packing area 3, the process water is saturated in the light hydrocarbon after being vaporized, partial pressure is provided by the light hydrocarbon under the condition of certain total pressure, the vaporization temperature of the process water is reduced, and the energy consumption of the device is reduced. Ethane is preferably fed, the pressure at the top of the light hydrocarbon feeding saturation tower 4 is 0.5MPa (g), the temperature at the top of the tower is 120 ℃, and the mass ratio (steam/ethane) is 0.3. The ethane after water saturation passes through the stainless steel defoaming net 2 to remove water drops carried in the gas phase, so that chemical media in the process water are prevented from entering the radiation furnace tube, particularly Na +, and the harm to the radiation furnace tube is reduced. The steam/ethane feed mixture enters a saturated feed superheater 16 and is superheated by low-pressure steam for 7 ℃, so that saturated steam in the steam/ethane feed mixture is prevented from condensing on the pipe wall to form two-phase flow in the flowing process, the pipe wall is washed, the steam/ethane ratio is reduced, and the heated steam/ethane feed mixture enters a cracking furnace 18.
The process water comes from a quenching water tower 19, the process water purified by a process water treatment unit 20 enters the lower part of a partition plate 6 of a light hydrocarbon feeding saturation tower 4, and fresh process water is heated by low-pressure steam in a circulating heater 17 through a process water circulating pump 10, distributed above a packing area 3, flows downwards along the packing and is vaporized by countercurrent contact with rising ethane. Preferably, the ethane feed is 200 t/h, the flow rate of the circulating process water is 960 t/h, the temperature is 138 ℃, and the overhead temperature of the light hydrocarbon feed saturation tower 4 is 120 ℃.
The process water in the light hydrocarbon feeding saturation tower 4 is continuously discharged to a boundary region sewage treatment system, the quality of the process water in the light hydrocarbon feeding saturation tower 4 is maintained, and soluble solids and salt in the process water are prevented from scaling on the filler to influence the performance of equipment.
The above embodiments are only used for illustrating the present invention, and not for limiting the present invention, and those skilled in the relevant technical field can make various changes and modifications without departing from the spirit and scope of the present invention, so that all equivalent technical solutions also belong to the scope of the present invention, and the protection scope of the present invention should be defined by the claims.
Claims (10)
1. A dilute steam generator for thermal cracking of light hydrocarbon capable of controlling steam/hydrocarbon ratio is characterized in that: the generating device mainly comprises a light hydrocarbon feeding saturation tower, a process water circulating pump, a circulating heater, a saturated feeding superheater and a sewage cooler; one side of the lower part of the light hydrocarbon feeding saturation tower is communicated with a light hydrocarbon feeding pipeline, the other side of the lower part of the light hydrocarbon feeding saturation tower is provided with a process water inlet, and the process water inlet is communicated with a process water inlet pipeline; the bottom of the light hydrocarbon feeding saturation tower is provided with a process water extraction port, and the process water extraction port is sequentially communicated with a process water circulating pump, a circulating heater and a process water inlet arranged at the upper part of the light hydrocarbon feeding saturation tower through pipelines; the bottom of the light hydrocarbon feeding saturated tower is also provided with a drain outlet which is communicated with a blowdown cooler, and the blowdown cooler is connected to a sewage treatment system; the top of the light hydrocarbon feeding saturation tower is provided with an outlet, the outlet is connected with a saturated feeding superheater, and the saturated feeding superheater is connected to the cracking furnace.
2. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 1, wherein: the light hydrocarbon feeding saturation tower is internally provided with a partition plate, a gas distributor, a packing area and a demister in sequence from bottom to top.
3. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 2, wherein: the process water inlet and the process water extraction port are arranged on the same side of the light hydrocarbon feeding saturation tower, the partition plate is arranged at the bottom of the light hydrocarbon feeding saturation tower, and the process water inlet, the process water extraction port and the sewage discharge port are separated by the partition plate.
4. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 3, wherein: the cross section of the partition plate is L-shaped, and a gap is reserved between the partition plate and the bottom of the light hydrocarbon feeding saturation tower, so that the two sides of the partition plate are communicated.
5. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 2, wherein: the gas distributor is arranged above the partition plate in the light hydrocarbon feeding saturation tower, and the light hydrocarbon feeding pipeline extends into the tower and then is connected to the gas distributor.
6. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 2, wherein: the packing area is arranged above the gas distributor in the light hydrocarbon feeding saturation tower, and bulk packing or regular packing is arranged in the packing area.
7. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 2, wherein: the demister is arranged above the packing area in the light hydrocarbon feeding saturation tower and is a stainless steel demister net.
8. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 2, wherein: the process water inlet is arranged between the packing area and the demister.
9. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 1, wherein: the top export of light hydrocarbon feeding saturation tower links to each other through ejection of compact pipeline between with the saturated feeding over heater, ejection of compact pipeline to light hydrocarbon feeding saturation tower direction slope, the slope of slope is 1/500 ~ 1/100.
10. The dilute steam generator for thermal cracking of light hydrocarbons with controllable steam-to-hydrocarbon ratio as claimed in claim 1, wherein: and the circulating heater and the saturated feeding superheater are heated by adopting low-pressure steam.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114275743A (en) * | 2021-12-10 | 2022-04-05 | 湖北兴福电子材料有限公司 | Method for producing high-purity liquid sulfur trioxide for electronic-grade sulfuric acid |
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2019
- 2019-08-30 CN CN201921431464.2U patent/CN210462963U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114275743A (en) * | 2021-12-10 | 2022-04-05 | 湖北兴福电子材料有限公司 | Method for producing high-purity liquid sulfur trioxide for electronic-grade sulfuric acid |
| CN114275743B (en) * | 2021-12-10 | 2023-04-28 | 湖北兴福电子材料股份有限公司 | Method for producing high-purity liquid sulfur trioxide for electronic-grade sulfuric acid |
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Effective date of registration: 20230510 Address after: Level 3, B4, No.10 Jiuxianqiao Road, Chaoyang District, Beijing, 100015 Patentee after: Sibierums Engineering Technology (Beijing) Co.,Ltd. Address before: 222065 room 323, building 2, Jiangsu Avenue SME Park, Xuwei New District, Lianyungang City, Jiangsu Province Patentee before: Lianyungang Petrochemical Co.,Ltd. |
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