CN110257100A - Light hydrocarbons humidification steam distribution system and method - Google Patents
Light hydrocarbons humidification steam distribution system and method Download PDFInfo
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- CN110257100A CN110257100A CN201910507329.XA CN201910507329A CN110257100A CN 110257100 A CN110257100 A CN 110257100A CN 201910507329 A CN201910507329 A CN 201910507329A CN 110257100 A CN110257100 A CN 110257100A
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- raw material
- conditioning tower
- material conditioning
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/80—Forming a predetermined ratio of the substances to be mixed
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of light hydrocarbons humidification steam distribution system and method, has used raw material conditioning Tower, process water stripper and pyrolysis furnace, and light hydrocarbon feedstock enters the lower part of raw material conditioning Tower by the preheating of pyrolysis furnace；The boosted rear lower part for entering raw material conditioning Tower of process water after being stripped in process water stripper；Liquid phase in raw material conditioning Tower by tower bottom through reflux pump and be heated at reflux device and return to raw material conditioning Tower top as spray liquid, exchange heat with the light hydrocarbon feedstock counter current contacting for entering raw material conditioning Tower lower part, form the mixing light hydro carbons raw material of saturation；The mixing light hydro carbons raw material of saturation by raw material conditioning Tower tower top pipeline through raw material superheater, eventually enter into the cracking section of pyrolysis furnace and generate cracking gas.
Description
Technical field
The present invention relates to the light hydrocarbons humidification steam distribution systems and method in cracking of ethylene technology.
Background technique
Currently, cracking of ethylene technology mainly passes through short residence time, high temperature, low hydrocarbon partial pressure (i.e. best dilution steam generation and hydrocarbon
Charge ratio) cracking load cases combination, carry out driving a reaction and balance to diene yield is improved, inhibit coking direction mobile.Flexible modulation
The ratio of dilution steam generation and raw material is the key technology of pyrolysis furnace.
Traditional unstripped gas matches Dilution steam system, as shown in Figure 1, having process water stripper 11, dilution steam generation to send out
Raw device 12 and pyrolysis furnace 13, process water enter process water stripper 11 by process water feed heater 14, are passed through by tower bottom
Dilution steam generation feed pump 15 boosts, then heats through dilution steam generation heater 16, into Dilution steam generator 12, the dilution of generation
After steam flows through dilution steam generation superheater 17, into pyrolysis furnace 13 convection section complete heat exchange, then with by each coil pipe and cracking
The convection section of furnace completes the raw material mixing of heat exchange, and the cracking section for finally entering pyrolysis furnace 13 forms cracking gas.
Wherein, Dilution steam generator generally uses two kinds of boiling hot sources again, and one is quench oil, another kind is steam.Such as
When fruit lightweight material cracks, heated only with steam.Dilution steam generation operating pressure is in 0.6~0.9MPaA, to meet dilution steam generation
The pressure requirements of raw material are mixed into, by the mass ratio (such as 0.3) of flow ratio control system dilution steam generation and raw material, are realized with vapour
Purpose.Limited by dilution steam generation operating pressure, such as using steam heat, generally use middle pressure steam, pressure limit be 0.9~
1.6MPaA。
Traditional handicraft uses pipeline mixed method, and steam direct heating moisturizing vaporization generates dilution steam generation, to reach mixing
The pressure rating of required pressure, steam is higher, is not available more low-grade heat source, and energy consumption is larger.
Separately there is patent CN90108341.0 to disclose a kind of saturation process of steam cracking feed gas, utilizes pipe type heat transfer
Device thermosiphon principle, unstripped gas and water enter tubulation from bottom to top, and outlet aqueous portion gasification is mixed with unstripped gas, realized former
Expect the saturation of gas.This method heats the two-phase mixture of water and unstripped gas by the flow of adjusting steam, and water section vaporizes, by
In the heat exchange of two-phase, and strict control outlet temperature is wanted, exchanges heat complex, be not easy to reach heat transfer requirements.
Summary of the invention
It is an object of the present invention to provide a kind of light hydrocarbons humidification steam distribution system and methods, on the one hand reduce the pressure of steam
Power grade reduces energy consumption, on the other hand makes system excessively complicated, enhances practicability.
To achieve the above object, the technical solution adopted by the present invention is that:
A kind of light hydrocarbons humidification steam distribution system, it is characterised in that: including raw material conditioning Tower, process water stripper and split
Solve furnace, in which:
Light hydrocarbon feedstock is connected to the lower part of raw material conditioning Tower by the preheating of pyrolysis furnace；
The lower part of raw material conditioning Tower is connected to after process water after stripping in process water stripper is boosted；
The tower bottom of raw material conditioning Tower is through reflux pump and is heated at reflux device and returns to the top of raw material conditioning Tower as spray
Liquid, to constitute circulation loop；
The tower top of raw material conditioning Tower is finally connected to the cracking section of pyrolysis furnace with pipeline through raw material superheater.
The light hydrocarbons are humidified steam distribution system, in which: the pipeline is first connected to the convection section of pyrolysis furnace, by the
After the heat exchange of one heat exchange coil and the second heat exchange coil, then it is connected to the cracking section of pyrolysis furnace.
The light hydrocarbons humidification steam distribution system, in which: raw material conditioning Tower is equipped with continuous blowdown pipeline, blowdown pipeline warp
Blow down cooler is connected to battery limit (BL).
A kind of light hydrocarbons humidification matches vapour method, it is characterised in that: used raw material conditioning Tower, process water stripper and
Pyrolysis furnace, in which:
Light hydrocarbon feedstock enters the lower part of raw material conditioning Tower by the preheating of pyrolysis furnace；
The boosted rear lower part for entering raw material conditioning Tower of process water after being stripped in process water stripper；
Liquid phase in raw material conditioning Tower through reflux pump and is heated at reflux device and returns to the top of raw material conditioning Tower by tower bottom
Circulation loop is constituted as spray liquid, light hydrocarbon feedstock and spray liquid counter current contacting into raw material conditioning Tower lower part are changed
Heat forms the mixing light hydro carbons raw material of saturation；
The mixing light hydro carbons raw material of saturation by raw material conditioning Tower tower top pipeline through raw material superheater, eventually enter into and split
It solves the cracking section of furnace and generates cracking gas.
The light hydrocarbons humidification matches vapour method, in which: the process water come from quenching water column removes trace solid
After hydrocarbon, enters process water stripper after the heating of process water feed heater, volatile component is stripped off in stripper and returns
Quenching water column is returned to, the process water after stripping enters the lower part of raw material conditioning Tower after feedstock pump boosting.
The described light hydrocarbons humidification matches vapour method, in which: the pipeline is first connected to the convection section of pyrolysis furnace, by the
After the heat exchange of one heat exchange coil and the second heat exchange coil, then it is connected to the cracking section of pyrolysis furnace.
The light hydrocarbons humidification matches vapour method, in which: the spray flow of raw material conditioning Tower and the mass ratio of unstripped gas
For 4-5, the water hydrocarbon mass ratio of the mixing light hydro carbons raw material of saturation is 0.2-0.4.
The light hydrocarbons humidification matches vapour method, in which: the operating pressure of the raw material conditioning Tower is in 0.4-1.0MPaA
In range, when operating pressure is constant, by adjusting the flow and/or temperature of the circulation loop, raw material conditioning Tower can be controlled
Operation temperature, to set the mass ratio of steam and unstripped gas, the mass ratio be in 0~1 in the range of.
The light hydrocarbons humidification matches vapour method, in which: the light hydrocarbon feedstock refers to ethane, propane, carbon four, carbon
Five mixture or pure material.
The light hydrocarbons humidification matches vapour method, in which: returns after being heated at reflux device heat exchange in the circulation loop
The temperature of the water of raw material conditioning Tower is within the scope of 120~165 DEG C.
The light hydrocarbons humidification matches vapour method, in which: the spray flow and entrance raw material conditioning Tower of the circulation loop
The quality spray ratio of the light hydrocarbon feedstock of lower part is in the range of 1-10.
System and method for provided by the invention, the raw material conditioning Tower are equipped with circulation loop, circulation loop using steam or
Other heat source indirect heat exchanges input heat, realize hot water with light hydrocarbon gas is inversely spraying mixes, to reach certain raw material
Dilution steam generation proportion.The System and method for operating principle is simple, the proportion of dilution steam generation easy to control, and tower exports water in gaseous mixture
It is the operating pressure of raw material conditioning Tower and the function of temperature, pressure (back pressure of pyrolysis furnace) with the ratio (thinner ratio) of unstripped gas
When constant, the operation temperature by controlling raw material conditioning Tower is that can reach the thinner ratio of needs.
System and method for provided by the invention returns to raw material conditioning Tower after being heated at reflux device heat exchange in the circulation loop
Water temperature within the scope of 120~165 DEG C, therefore be heated at reflux device and can be used compared with low-grade heat source, it is traditional dilute to substitute
Release steam generator system；Using the middle pressure steam in low-grade low-pressure steam substitution traditional handicraft, 10~20,000 can be saved
Gram mark oil/ton ethylene, to reach energy-efficient purpose.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of traditional raw material gas proportion Dilution steam system；
Fig. 2 is the structural schematic diagram of light hydrocarbons humidification steam distribution system provided by the invention.
Description of symbols: process water stripper 11；Dilution steam generator 12；Pyrolysis furnace 13；Process water charging heating
Device 14；Dilution steam generation feed pump 15；Dilution steam generation heater 16；Dilution steam generation superheater 17；Raw material conditioning Tower 21；Technique steam
Stripper 22；Pyrolysis furnace 23；Preheat coil pipe 231；First heat exchange coil 232；Second heat exchange coil 233；Process water feed heater
24；Feedstock pump 25；Process water stripper reboiler 26；Reflux pump 27；It is heated at reflux device 28；Blow down cooler 29；Raw material
Superheater 30.
Specific embodiment
Hereinafter reference will be made to the drawings is described in detail by way of example and not limitation some specific embodiments of the present invention.
Identical appended drawing reference denotes same or similar part or part in attached drawing.It should be appreciated by those skilled in the art that these
Attached drawing is not necessarily to be depicted true to scale.
Below in conjunction with shown in Fig. 2, introducing a kind of light hydrocarbons humidification steam distribution system provided by the invention and method, the system
System includes raw material conditioning Tower 21, process water stripper 22 and pyrolysis furnace 23, in which:
Light hydrocarbon feedstock becomes superheated feedstock after the preheating by the preheating coil pipe 231 of pyrolysis furnace 23, into raw material
The lower part of conditioning Tower 21；
The process water come from quenching water column heats laggard after removing trace solid and hydrocarbon through process water feed heater 24
Enter process water stripper 22, volatile component is stripped off in technique stripper 22 and returns to quenching water column, the technique after stripping
Water (118 DEG C of temperature, operating pressure 0.15MPaA, flow 66t/h) enters raw material conditioning Tower 21 after 25 boosting of feedstock pump
The lower part of (131 DEG C of tower top temperature, 106 DEG C of column bottom temperature, operating pressure 0.82MPaA), the tower bottom liquid phase warp of raw material conditioning Tower 21
Raw material humidification is returned after reflux pump 27 (flow 900t/h) pressurization, after being heated at reflux the heating of device 28 (140 DEG C of outlet temperature)
Tower 21 as spray liquid (constitute circulation loop), in inner-tower filling material bed 211 with the superheated feedstock (temperature from pyrolysis furnace 23
150 DEG C, flow 200t/h) counter current contacting；(131 DEG C of temperature, flow mixing light hydro carbons raw material in raw material conditioning Tower 21 after saturation
Measure 260t/h) pyrolysis furnace 23 is returned after the overheat (140 DEG C of temperature) of raw material superheater 30 from the tower top of raw material conditioning Tower 21
Convection section；The subsequent processing path of mixing light hydro carbons raw material after overheat and processing method are same as the prior art, that is,
In the convection section of pyrolysis furnace 23 after the heat exchange of the first heat exchange coil 232 and the second heat exchange coil 233, into pyrolysis furnace 23
It cracks section and forms cracking gas.
Wherein, the mass ratio of the reflux spray flow of raw material conditioning Tower 21 and unstripped gas is 4.5, mixing light hydro carbons raw material
After humidification saturation is with vapour, water hydrocarbon mass ratio is 0.3；
Moreover, raw material conditioning Tower 21 is equipped with continuous blowdown pipeline, sewerage is sent after blow down cooler 29 is cooled to 40 DEG C
To battery limit (BL).
System and method for provided by the invention, the raw material conditioning Tower are equipped with circulation loop, circulation loop using steam or
Other heat source indirect heat exchanges input heat, realize hot water with light hydrocarbon gas is inversely spraying mixes, to reach certain raw material
Dilution steam generation proportion.The System and method for operating principle is simple, the proportion of dilution steam generation easy to control, and tower exports water in gaseous mixture
It is the operating pressure of raw material conditioning Tower and the function of temperature, pressure (back pressure of pyrolysis furnace) with the ratio (thinner ratio) of unstripped gas
When constant, the operation temperature by controlling raw material conditioning Tower is that can reach the thinner ratio of needs.
System and method for provided by the invention compared with low-grade heat source, it can be achieved that utilize, alternative traditional dilution steam generation hair
Raw device system can save 10~20 kilograms of mark oil/tons using the middle pressure steam in low-grade low-pressure steam substitution traditional handicraft
Ethylene, to reach energy-efficient purpose.
System and method for provided by the invention, light hydrocarbon feedstock refer to ethane, propane, carbon four, the mixture of light dydrocarbon etc.
Or pure material.
System and method for provided by the invention, the operating pressure of raw material conditioning Tower is within the scope of 0.4-1.0MPaA, operation pressure
When power is constant, by the flow and/or temperature of the adjusting circulation loop, the operation temperature of raw material conditioning Tower can be controlled, with
The mass ratio of steam and unstripped gas is set, which is in the range of 0~1.
Low-grade steam or other low-grade heats can be used in System and method for provided by the invention, the device that is heated at reflux
Source meets the temperature of the water of circulation loop return raw material conditioning Tower within the scope of 120~165 DEG C, i.e., the water of circulation loop is through changing
It is not undergone phase transition after heat.
System and method for provided by the invention, the spray flow of the circulation loop and the lightweight for entering raw material conditioning Tower lower part
The quality spray ratio of hydrocarbon raw material is in the range of 1-10.
Described above to be merely exemplary for the purpose of the present invention, and not restrictive, those of ordinary skill in the art understand,
Without departing from the spirit and scope defined by the claims, can many modifications may be made, variation or equivalent, but will all fall
Enter within protection scope of the present invention.
Claims (11)
- The steam distribution system 1. a kind of light hydrocarbons are humidified, it is characterised in that: including raw material conditioning Tower, process water stripper and cracking Furnace, in which:Light hydrocarbon feedstock is connected to the lower part of raw material conditioning Tower by the preheating of pyrolysis furnace；The lower part of raw material conditioning Tower is connected to after process water after stripping in process water stripper is boosted；The tower bottom of raw material conditioning Tower is through reflux pump and is heated at reflux device and returns to the top of raw material conditioning Tower as spray liquid, with Constitute circulation loop；The tower top of raw material conditioning Tower is finally connected to the cracking section of pyrolysis furnace with pipeline through raw material superheater.
- The steam distribution system 2. light hydrocarbons according to claim 1 are humidified, it is characterised in that: the pipeline is first connected to cracking The convection section of furnace after the heat exchange of the first heat exchange coil and the second heat exchange coil, then is connected to the cracking section of pyrolysis furnace.
- The steam distribution system 3. light hydrocarbons according to claim 1 are humidified, it is characterised in that: raw material conditioning Tower is equipped with continuous row Dirty pipeline, blowdown pipeline are connected to battery limit (BL) through blow down cooler.
- 4. a kind of light hydrocarbons humidification matches vapour method, it is characterised in that: used raw material conditioning Tower, process water stripper and split Solve furnace, in which:Light hydrocarbon feedstock enters the lower part of raw material conditioning Tower by the preheating of pyrolysis furnace；The boosted rear lower part for entering raw material conditioning Tower of process water after being stripped in process water stripper；Liquid phase in raw material conditioning Tower through reflux pump and is heated at reflux device and returns to the top conduct of raw material conditioning Tower by tower bottom Spray liquid and constitute circulation loop, into raw material conditioning Tower lower part light hydrocarbon feedstock and the spray liquid counter current contacting exchange heat, Form the mixing light hydro carbons raw material of saturation；The mixing light hydro carbons raw material of saturation by raw material conditioning Tower tower top pipeline through raw material superheater, eventually enter into pyrolysis furnace Cracking section and generate cracking gas.
- 5. light hydrocarbons humidification according to claim 4 matches vapour method, it is characterised in that: the work come from quenching water column Skill water after removing trace solid and hydrocarbon, enters process water stripper, the vapour in stripper after the heating of process water feed heater It is proposed that volatile component returns to quenching water column, the process water after stripping enters raw material conditioning Tower after feedstock pump boosting Lower part.
- 6. light hydrocarbons humidification according to claim 4 matches vapour method, it is characterised in that: the pipeline is first connected to cracking The convection section of furnace after the heat exchange of the first heat exchange coil and the second heat exchange coil, then is connected to the cracking section of pyrolysis furnace.
- 7. light hydrocarbons according to claim 4 humidification matches vapour method, it is characterised in that: the spray flow of raw material conditioning Tower with The mass ratio of unstripped gas is 4-5, and the water hydrocarbon mass ratio of the mixing light hydro carbons raw material of saturation is 0.2-0.4.
- 8. light hydrocarbons humidification according to claim 4 matches vapour method, it is characterised in that: the operation of the raw material conditioning Tower Pressure is within the scope of 0.4-1.0MPaA, when operating pressure is constant, by adjusting the flow and/or temperature of the circulation loop, energy The operation temperature of raw material conditioning Tower is enough controlled, to set the mass ratio of steam and unstripped gas, which is in 0~1 In range.
- 9. light hydrocarbons humidification according to claim 4 matches vapour method, it is characterised in that: the light hydrocarbon feedstock refers to Ethane, propane, carbon four, light dydrocarbon mixture or pure material.
- 10. light hydrocarbons humidification according to claim 4 matches vapour method, it is characterised in that: passed through back in the circulation loop The temperature that the water of raw material conditioning Tower is returned after heater exchanges heat is flowed within the scope of 120~165 DEG C.
- 11. light hydrocarbons humidification according to claim 4 matches vapour method, it is characterised in that: the spray of the circulation loop The mass ratio with the light hydrocarbon feedstock for entering raw material conditioning Tower lower part is measured in the range of 1-10.
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| CN201910507329.XA CN110257100A (en) | 2019-06-12 | 2019-06-12 | Light hydrocarbons humidification steam distribution system and method |
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| CN201910507329.XA CN110257100A (en) | 2019-06-12 | 2019-06-12 | Light hydrocarbons humidification steam distribution system and method |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040004022A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Process for steam cracking heavy hydrocarbon feedstocks |
| CN102057018A (en) * | 2008-06-10 | 2011-05-11 | 埃克森美孚化学专利公司 | Process and apparatus for cooling liquid bottoms from vapor-liquid separator by heat exchange with feedstock during steam cracking of hydrocarbon feedstocks |
| CN107344906A (en) * | 2016-05-06 | 2017-11-14 | 中国石化扬子石油化工有限公司 | A kind of method that ethene is prepared using tube cracking furnace |
| CN210163383U (en) * | 2019-06-12 | 2020-03-20 | 中国寰球工程有限公司 | Light hydrocarbon humidifying and steam distributing system |
-
2019
- 2019-06-12 CN CN201910507329.XA patent/CN110257100A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20040004022A1 (en) * | 2002-07-03 | 2004-01-08 | Stell Richard C. | Process for steam cracking heavy hydrocarbon feedstocks |
| CN102057018A (en) * | 2008-06-10 | 2011-05-11 | 埃克森美孚化学专利公司 | Process and apparatus for cooling liquid bottoms from vapor-liquid separator by heat exchange with feedstock during steam cracking of hydrocarbon feedstocks |
| CN107344906A (en) * | 2016-05-06 | 2017-11-14 | 中国石化扬子石油化工有限公司 | A kind of method that ethene is prepared using tube cracking furnace |
| CN210163383U (en) * | 2019-06-12 | 2020-03-20 | 中国寰球工程有限公司 | Light hydrocarbon humidifying and steam distributing system |
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Inventor after: Zhang Laiyong Inventor after: Liu Jianguo Inventor after: Cao Yuanwei Inventor after: Jin Zhuoyi Inventor after: Zhao Zhiqiang Inventor after: Wang Yunhui Inventor after: Xin Jiang Inventor after: Wu Dejuan Inventor after: Sun Changgeng Inventor after: Ji Jinghua Inventor after: Yang Qinglan Inventor after: Hu Zhongcai Inventor after: Zhao Hongxia Inventor after: Lu Wenhua Inventor before: Xin Jiang Inventor before: Cao Yuanwei Inventor before: Jin Zhuoyi Inventor before: Zhao Zhiqiang Inventor before: Wang Yunhui Inventor before: Wu Dejuan Inventor before: Sun Changgeng Inventor before: Ji Jinghua Inventor before: Yang Qinglan Inventor before: Hu Zhongcai Inventor before: Zhao Hongxia Inventor before: Lu Wenhua Inventor before: Liu Jianguo |
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