CN110819377B - Process method for improving light hydrocarbon feeding of ethylene unit cracking furnace - Google Patents
Process method for improving light hydrocarbon feeding of ethylene unit cracking furnace Download PDFInfo
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- CN110819377B CN110819377B CN201911068941.8A CN201911068941A CN110819377B CN 110819377 B CN110819377 B CN 110819377B CN 201911068941 A CN201911068941 A CN 201911068941A CN 110819377 B CN110819377 B CN 110819377B
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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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
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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
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
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- Thermal Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention belongs to the technical field of improved processes of ethylene devices, and particularly relates to a process method for improving light hydrocarbon feeding of an ethylene device cracking furnace, which is characterized in that mixed circulating ethane and propane with too low temperature are introduced into a standby LPG evaporator (2), heated and then merged into an LPG superheater (4), and then merged with an outlet pipeline of a circulating C3-C2 superheater (1) to enable the temperature to reach 75-80 ℃ and then enter the light hydrocarbon furnace.
Description
Technical Field
The invention belongs to the technical field of ethylene unit improvement processes, and particularly relates to a process method for improving light hydrocarbon feeding of an ethylene unit cracking furnace.
Background
The ethylene device is a tap device in the petrochemical industry, and the capacity of the ethylene device marks the development level of the national petrochemical industry. In recent years, the domestic ethylene industry has been rapidly developed and becomes the second major ethylene producing country around the world. In daily application production, due to the fact that the feeding temperature of the light hydrocarbon furnace is too low, dew point corrosion of a pipeline at the preheating section of the light hydrocarbon furnace is caused, the light hydrocarbon pipeline can be leaked after the light hydrocarbon furnace is seriously corroded, and great potential safety hazards exist.
Disclosure of Invention
In order to solve the technical problems, the invention aims to provide a process method for feeding light hydrocarbon into a cracking furnace of an ethylene unit;
the purpose of the invention can be realized by the following technical scheme:
a process method for improving light hydrocarbon feeding of an ethylene unit cracking furnace adopts the steps that mixed circulating ethane and propane with low temperature are introduced into a standby LPG evaporator (2), heated and then merged into an LPG superheater (4), and then merged with an outlet pipeline of a circulating C3-C2 superheater (1) to reach the temperature of 75-80 ℃ and enter a light hydrocarbon furnace.
The method is specifically operated as follows: leading 16t/h of C2 and C3 mixed gas in front of inlets of circulating C2 and C3 superheaters (1) out for 8t/h to enter a standby LPG evaporator (2), wherein the standby LPG evaporator (2) is connected with an LPG evaporator (3) in parallel, the standby LPG evaporator (2) is provided with a condensate line (5) connected to an outlet line of the LPG superheater (4), and a liquid level regulating valve is arranged at a condensate outlet; the mixed gas of C2 and C3 at the outlet of the spare LPG evaporator (2) and the LPG at the outlet of the LPG evaporator (3) are mixed and then enter the LPG superheater (4), finally, the temperature of the mixed gas of C2 and C3 at the outlet of the circulating C3-C2 superheater (1) is increased to 56-58 ℃, and the temperature of the mixed gas of C2 and C3 at the outlet of the circulating C3-C2 superheater (1) and the mixed gas of C2, C3 and LPG at the outlet of the spare LPG evaporator (2) and the LPG evaporator (3) is 75-80 ℃.
The 16t/h C2 and C3 mixed gas is specifically as follows: the 2t/h circulating propane is subjected to heat exchange with low-pressure steam through a heat exchanger (12) and then mixed with 12t/h circulating ethane and 2t/h oilfield ethane.
The temperature of the mixture of C2 and C3 at the outlet of the circulating C3-C2 superheater (1) is controlled by controlling a flow regulating valve (7) to regulate the amount of condensate according to the indication of a temperature remote transmission element (6).
The temperature of the mixed gas at the outlet of the LPG superheater (4) is controlled to 88-90 ℃, and the temperature can be controlled by adjusting the amount of condensate through a first liquid level adjusting valve (8) and a second liquid level adjusting valve (9).
The control temperature specifically comprises the following steps: the first liquid level regulating valve (8) is interlocked with the third liquid level remote transmission element (13) and the temperature remote transmission element (10), the liquid level regulating valve (8) is switched on and off according to the temperature indicated by the temperature remote transmission element (10), and because the condensate at the outlet of the LPG evaporator (3) is the condensate inlet of the LPG superheater (4), the liquid level regulating valve (9) can be controlled according to the temperature indicated by the temperature remote transmission element (10) to enable the outlet of the LPG superheater (4) to reach 88-90 ℃.
The temperature of the mixed gas of C2 and C3 at the outlet of the circulating C3-C2 superheater (1) and the temperature of the mixed gas of C2, C3 and LPG at the outlet of the standby LPG evaporator (2) and the LPG evaporator (3) can be indicated by an interlocking temperature remote indication element (11).
The invention has the beneficial effects that:
the process method solves the problems of over-low feeding temperature of the light dydrocarbon furnace, dew point corrosion of a pipeline at the preheating section of the light dydrocarbon furnace, leakage of the light dydrocarbon pipeline and the like.
Drawings
In order to facilitate understanding for those skilled in the art, the present invention will be further described with reference to the accompanying drawings.
FIG. 1 is a partial structural view of the process of the present invention.
Detailed Description
The invention is illustrated in detail by the following examples in conjunction with fig. 1:
example 1:
the feeding of the light hydrocarbon before the modification is mixed feeding of C2, C3 (circulating ethane and circulating propane) and LPG, wherein the feeding of the mixed gas of C2 and C3 is 16t/h, and the feeding of LPG is 6-8 t/h. The 2t/h circulating propane exchanges heat with low-pressure steam through a heat exchanger 12, is mixed with 12t/h circulating ethane and 2t/h oilfield ethane (total 16t/h), and then enters a circulating C3-C2 superheater (1), and the outlet temperature of mixed gas of C2 and C3 is about 45 ℃. The temperature of an outlet of the LPG is about 95 ℃ after the LPG enters an LPG evaporator (3) from a boundary area to exchange heat with low-pressure steam and then enters an LPG superheater (4) to exchange heat with low-pressure condensate without exchanging heat. The mixed gas of the C2, the C3 and the LPG enters the furnace at the temperature of about 50 ℃.
Through calculation, the 16t/h mixed gas of C2 and C3 in front of the inlet of the circulating C3-C2 superheater (1) needs to be led out 8t/h and enters the standby LPG evaporator (2) added in the overhaul period, and meanwhile, the standby LPG evaporator (2) is additionally provided with a condensate line (5) to the condensate outlet of the LPG superheater (4) and a liquid level regulating valve. Mixed gas at outlets C2 and C3 of a spare LPG evaporator (2) and LPG at an outlet of an LPG evaporator (3) are mixed and then enter an LPG superheater (4), so that the temperature of the mixed gas at outlets C2 and C3 of a circulating C3-C2 superheater (1) can be increased to about 56 ℃ after modification, and the temperature can be controlled by controlling a flow regulating valve (7) to regulate the amount of condensate according to the indication of a temperature remote transmission (11); the temperature of the mixed gas at the outlets of the LPG superheater (4) and the standby LPG evaporator (2) reaches about 88 ℃, and finally the temperature of the mixed gas at the outlets of the circulating C3-C2 superheater (1) C2 and C3, the mixed gas at the outlets of the LPG superheater (4) and the standby LPG evaporator (2) C2 and C3 and the mixed gas at the outlets of the standby LPG evaporators is 75-80 ℃.
The temperature of mixed gas at the outlet of the LPG superheater (4) can reach about 88 ℃ through control, the temperature can be controlled by adjusting the amount of condensate through a first liquid level adjusting valve (8) and a second liquid level adjusting valve (9) (the first liquid level adjusting valve (8), a third liquid level remote transmission element (13) and a temperature remote transmission element (10) are interlocked, the liquid level adjusting valve (8) is switched on and off according to the temperature indicated by the temperature remote transmission element (10), the condensate at the outlet of the LPG evaporator (3) is the condensate inlet of the LPG superheater (4), so the liquid level adjusting valve (9) can be controlled according to the temperature indicated by the temperature remote transmission element (10) to ensure that the outlet of the LPG (4) reaches 88 ℃, and finally the C2, C3 mixed gas at the outlet of a circulating C3-C2 (1) and a standby LPG evaporator (2), the outlet C2, C3, C3 and LPG, The combined temperature of the LPG mixed gas is 75-80 ℃ (the temperature after mixing can be indicated by an interlocking temperature remote indication element (11)).
The preferred embodiments of the invention disclosed above are intended to be illustrative only. The preferred embodiments are not intended to be exhaustive or to limit the invention to the precise embodiments disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and the practical application, to thereby enable others skilled in the art to best utilize the invention. The invention is limited only by the claims and their full scope and equivalents.
Claims (5)
1. A process method for improving light hydrocarbon feeding of an ethylene unit cracking furnace is characterized in that mixed circulating ethane and propane with low temperature are introduced into a standby LPG evaporator (2), heated and then merged into an LPG superheater (4), and then merged with an outlet pipeline of a circulating C3-C2 superheater (1) to enable the temperature to reach 75-80 ℃ and then enter a light hydrocarbon furnace;
the method is specifically operated as follows: leading 16t/h of mixed gas of C2 and C3 in front of an inlet of a circulating C3-C2 superheater (1) out for 8t/h and entering a standby LPG evaporator (2), wherein the standby LPG evaporator (2) is connected with an LPG evaporator (3) in parallel, the standby LPG evaporator (2) is provided with a condensate line (5) connected to the LPG superheater (4), and a liquid level regulating valve is arranged at a condensate outlet; c2 and C3 mixed gas at the outlet of the spare LPG evaporator (2) is mixed with LPG at the outlet of the LPG evaporator (3) and then jointly enters an LPG superheater (4), finally, the temperature of C2 and C3 mixed gas at the outlet of the circulating C3-C2 superheater (1) is increased to 56-58 ℃, and the temperature of the mixed gas of C2 and C3 at the outlet of the circulating C3-C2 superheater (1) is 75-80 ℃ after being combined with C2, C3 and LPG mixed gas at the outlets of the spare LPG evaporator (2) and the LPG evaporator (3);
the 16t/h C2 and C3 mixed gas is specifically as follows: the 2t/h circulating propane is subjected to heat exchange with low-pressure steam through a heat exchanger (12) and then mixed with 12t/h circulating ethane and 2t/h oilfield ethane.
2. The process for improving light hydrocarbon feeding of an ethylene unit cracking furnace as claimed in claim 1, wherein the temperature of the mixture of C2 and C3 at the outlet of the circulating C3-C2 superheater (1) is controlled by controlling the flow regulating valve (7) to regulate the amount of condensate according to the indication of the first temperature remote transmission element (6).
3. The process for improving light hydrocarbon feeding of an ethylene unit cracking furnace as claimed in claim 1, wherein the temperature of the mixed gas at the outlet of the LPG superheater (4) is controlled to 88-90 ℃, and the temperature can be controlled by adjusting the amount of condensate through the first liquid level adjusting valve (8) and the second liquid level adjusting valve (9).
4. The process of claim 3, wherein the controlling temperature is specifically operated to: the first liquid level regulating valve (8) is interlocked with the third liquid level remote transmission element (13) and the temperature remote transmission element (10), the first liquid level regulating valve (8) is switched on and off according to the temperature indicated by the temperature remote transmission element (10), and because the condensate at the outlet of the LPG evaporator (3) is the condensate inlet of the LPG superheater (4), the second liquid level regulating valve (9) can be controlled according to the temperature indicated by the temperature remote transmission element (10) to enable the outlet of the LPG superheater (4) to reach 88-90 ℃.
5. The process for improving light hydrocarbon feeding of an ethylene unit cracking furnace as claimed in claim 1, wherein the temperature of the combined C2 and C3 mixed gas at the outlet of the circulating C3-C2 superheater (1) and the combined C2, C3 and LPG mixed gas at the outlet of the standby LPG evaporator (2) and LPG evaporator (3) can be indicated by the interlocking temperature remote indication element (11).
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| CN201911068941.8A CN110819377B (en) | 2019-11-05 | 2019-11-05 | Process method for improving light hydrocarbon feeding of ethylene unit cracking furnace |
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| CN201911068941.8A CN110819377B (en) | 2019-11-05 | 2019-11-05 | Process method for improving light hydrocarbon feeding of ethylene unit cracking furnace |
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| US6441263B1 (en) * | 2000-07-07 | 2002-08-27 | Chevrontexaco Corporation | Ethylene manufacture by use of molecular redistribution on feedstock C3-5 components |
| CN103086821B (en) * | 2011-10-28 | 2015-10-21 | 中国石油化工股份有限公司 | A kind of production method of low-carbon alkene |
| CN107879876B (en) * | 2016-09-30 | 2020-07-24 | 中国石油化工股份有限公司 | Method and device for producing ethylene and propylene from light hydrocarbon raw material |
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