CN105566029B - A kind of method for reducing ethylene unit energy consumption - Google Patents
A kind of method for reducing ethylene unit energy consumption Download PDFInfo
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- CN105566029B CN105566029B CN201410542718.3A CN201410542718A CN105566029B CN 105566029 B CN105566029 B CN 105566029B CN 201410542718 A CN201410542718 A CN 201410542718A CN 105566029 B CN105566029 B CN 105566029B
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Abstract
The invention discloses a kind of method for reducing ethylene unit energy consumption, it is characterised in that the cracking gas of cracking outlet of still sends into oil scrubber after being cooled down through quencher, carries out material separation, and quench oil is drawn from oil scrubber bottom of towe, and part quench oil is sent to quencher；Part quench oil returns to oil scrubber；Part quench oil enters extraction tower and carries out solvent extraction, and extraction tower tower top material returns to oil scrubber, and extraction tower materials at bottom of tower pitch is mutually drawn, and wherein solvent used in extraction tower is the cracking gas that ethylene device compressor is exported.
Description
Technical field
It is to be related to a kind of method for reducing ethylene unit energy consumption furtherly the present invention relates to ethylene production field.
Background technology
At present, main ethylene unit produces ethene, propylene, butadiene, aromatic hydrocarbons etc. using steam thermal cracking process in the world
Basic organic chemical raw material.The raw materials such as lighter hydrocarbons, naphtha, hydrogenation tail oil are blended in industrial crack with a certain proportion of dilution steam generation
Occur cracking reaction in stove under hot conditions, pyrolysis product through the process final production such as over-quenching, compression, separation go out ethene,
The industrial chemicals such as propylene, butadiene.
Chilling system is the throat of ethylene unit, and it is made up of equipment such as quencher, oil scrubber, water scrubbers, is carry point
From cracking distillate (gasoline, diesel oil, fuel oil) component and the task of recovery process water, while still reclaiming heat in cracking process
The key equipment of amount.The cracking gas that the outlet of industrial pyrolysis furnace waste heat boiler comes sends into oil in quencher after quench oil spraying cooling
Tower bottom is washed, after backflow cooling, the light component in pyrolysis product continues cool to 40 from oil scrubber Base top contact into water scrubber
DEG C or so, into follow-up compression piece-rate system.
Most of dilution steam generation required for cracking process is all from the UTILIZATION OF VESIDUAL HEAT IN of quench oil inside device, and minority is not
Foot point is supplemented by pipe network steam.Oil scrubber bottom temperature is higher, steam generation it is more, device by utilizing waste heat is outer to mend using better
Steam consumption is fewer.Therefore the height of oil scrubber bottom temperature directly determines the size of waste heat recovery volume, the fortune of chilling system
The bad energy consumption height to ethylene unit of acting charitably has important influence, so as to also contribute to the production cost of device.
Regard ethylene unit chilling system as an entirety, inflow is pyrolysis product, and outflow is cracking gas and cracking
Distillate；Quench oil, process water etc. are in system interior circulation.Therefore ethylene unit chilling system, which runs well, will ensure two
Balance, heat balance, material balance.Heat balance is that the heat for bringing chilling system into by cracking gas will be by occurring dilution steam generation
Utilize Deng heat exchange mode.Material balance is then relative complex, because pyrolysis product, which enters, can occur polymerization etc. instead after chilling system
Should, change is produced, chilling system needs the pyrolysis product after change to discharge, to keep component in chilling system stable.
The practical problem of ethylene quenching system now in production is exactly that oil scrubber bottom temperature is low, and chilling oil viscosity is high.It is anxious
Cold oil bottom temperature is low, and dilution steam generation temperature difference of heat exchanger is small, dilution steam generation generating capacity wretched insufficiency, it is therefore desirable to which a large amount of steam are mended
Enter system；Chilling oil viscosity is high, and the power consumption of quenching oil circulation pump is high, causes ethylene unit energy consumption to remain high, when viscosity is too high
Can also blocking pipeline cause parking.
The reason for causing ethylene quenching system problem is exactly that the asphalitine generated in quench oil can not be discharged in time.In order to
Quench oil is circulated between quencher and oil wash tower reactor in the cracking gas cooling that pyrolysis furnace is produced, chilling system, and its internal circulating load is past
It is past to reach thousands of tphs, and the extraction for cracking distillate only has tens tphs, quench oil is stagnant for a long time in system
Stay, produce a large amount of asphalitines, viscosity is significantly raised.And in order to control chilling oil viscosity, oil wash bottom temperature can only be reduced to subtract
The speed of few asphalitine generation.But oil wash bottom temperature is reduced in the case of pyrolysis furnace load identical, quench oil can be increased
Internal circulating load, so that the time that quench oil is detained in system is longer, adds the amount of asphalitine generation again.So actual production
In oil wash bottom temperature can only be maintained to 180 DEG C or so, just can guarantee that the pitch of the asphalitine that is generated in quench oil and discharge
Matter balances each other, and maintains quench oil viscosity stabilization.Here it is 210 DEG C of oil scrubber tower reactor design temperature, can actual motion less than 190 DEG C
Basic reason.
At present, can only using adding quenched flux oil, adding viscosity reductant and using three kinds of methods of visbreaking tower on commercial plant
Chilling oil viscosity is controlled as cost, reluctantly to reduce oil scrubber bottom temperature, causes ethylene unit energy consumption to remain high.
First method is to add quenched flux oil (pyrolysis gas oil) reduction viscosity, largely pyrolysis gas oil will be blended to urgency
In cold oil, its side effect is very big.First, internal circulating load of the pyrolysis gas oil in oil scrubber can be increased, oil scrubber tower reactor is increased to tower
The gas phase load at middle part, correspondingly reduces the disposal ability of oil scrubber；Secondly, in pyrolysis gas oil containing substantial amounts of styrene,
The components such as naphthalene, indenes, when they are circulated with quench oil, it may occur that polymerisation produces polymer, and accumulates in oil scrubber
On column plate or filler, heat transfer and the mass transfer effect of influence column plate and filler rise tower pressure difference, and the disposal ability of tower declines；Again
It is secondary, due to the increase of pyrolysis gas oil internal circulating load, part can be contained in the Pyrolysis fuel oil PFO of drippolene and the tower reactor extraction of tower top
The component of diesel oil, has influence on the quality of drippolene and fuel oil, and the operation of follow-up quenching water column can be caused to deteriorate when serious；
Finally, due to the amount of quench oil is very big, therefore in order to reduce the viscosity of quench oil, it usually needs substantial amounts of cracking bavin is mixed for a long time
Oil.In this way, it is impossible to reduce asphalitine growing amount, chilling oil viscosity can only be typically controlled in 1000~2000mm2/s
(50 DEG C), oil scrubber bottom temperature is without significantly improving.
Viscosity reductant be in recent years domestic and international research department and ethene patent business work out it is various it is suitable reduction quench oils glue
The chemical agent of degree, visbreaking target is realized by adding the activity of chemical assistant suppression polymerisation free radical.CN
101062880A proposes a kind of Reduce viscosity agent being made up of polymerization inhibitor, dispersant and matal deactivator, polymerize with suppression,
Prevent aggregation and the effect of passivating metallic surfaces.Although add viscosity reductant reduces the formation speed of asphalitine to a certain extent,
It is not have any help to asphalitine discharge chilling system, it is impossible to fundamentally solve chilling oil viscosity height and oil scrubber tower reactor temperature
The problem of spending low.Viscosity reductant is seldom used alone in actual use, is while using visbreaking tower technology, to be made with viscosity reductant
For supplementary means.
Visbreaking tower technology is the quench oil that will be exported from quenching oil circulation pump, under the control of temperature control valve (TCV), with
The ethane cracking gas that Control for Pyrolysis Furnace Area is come is contacted in nozzle mixer, and the light component in quench oil is vaporized, with cracking gas
Into visbreaking tower.The light component vaporized in ethane cracking gas and quench oil enters oil scrubber tower reactor, non-vapour from visbreaking column overhead
The heavy liquid phase component of change enters visbreaking tower tower reactor, and tank field is output to as byproduct (Pyrolysis fuel oil PFO).So, it is selective
Ground fractionates out the heavier feeds containing more asphalitine from quench oil and stays light material in systems, makes circulation quench oil
In light components concentration increase, so as to reduce quench oil viscosity.But in fact, visbreaking column overhead temperatures are at 250-290 DEG C, only
Light component below this temperature can be returned to the component for there are a large amount of low viscosities in oil scrubber, the fuel oil of discharge, pitch is discharged
Efficiency it is low.Simultaneously as quench oil will be contacted with 500 DEG C or so of ethane stove cracking gas, stop add urgency at high temperature
Cold oil studies on asphaltene growing amount, is adversely affected to chilling oil viscosity., can only be by oil scrubber bottom temperature in actual motion
180 DEG C or so are limited in, chilling oil viscosity can be just controlled.
Prior art can only reduce oil scrubber tower reactor due to that effectively can not discharge the asphalitine generated in quench oil
Temperature controls chilling oil viscosity, considerably increases ethylene unit energy consumption.Especially, cracking stock progressively lighting in recent years, by
Seldom in the Pyrolysis fuel oil PFO of generation, i.e., discharge rate is smaller under identical internal circulating load, that is to say, that quench oil is detained in system
Time is longer, and the asphalitine of generation is more, and what can be discharged is less so that prior art loses effect substantially.Therefore, it is badly in need of out
Send out technology a kind of, reduce chilling oil viscosity, improve quenching oil column bottom temperature, reduce ethylene unit comprehensive energy consumption.
The content of the invention
To solve problems of the prior art, the invention provides a kind of method for reducing ethylene unit energy consumption.It is logical
Crossing solvent extraction reduces the viscosity of quench oil, by improving oil scrubber bottom temperature to improve chilling oil temperature, and then increases dilute
Steam production is released, using the cracking gas of compressor outlet as solvent, solvent consumption and compression power consumption is reduced, reduces ethylene unit
Comprehensive energy consumption.
It is an object of the invention to provide a kind of method of above-mentioned reduction ethylene unit energy consumption, it is characterised in that cracking
The cracking gas that outlet of still comes sends into oil scrubber after being cooled down through quencher, carry out material separation, and quench oil is drawn from oil scrubber bottom of towe,
Part quench oil is sent to quencher；Part quench oil returns to oil scrubber；Part quench oil enters extraction tower and carries out solvent extraction, extracting
Column overhead material returns to oil scrubber, and extraction tower materials at bottom of tower pitch is mutually drawn, and wherein solvent used in extraction tower fills for ethene
Put the cracking gas of compressor outlet.
The oil scrubber bottom temperature of the present invention brings up to 190-250 DEG C, is preferably increased to 195-235 DEG C.
During extraction tower solvent extraction, the weight ratio of solvent and quench oil is 0.01-20, preferably 0.5-5；Extract pressure tower
For 0.5MPa-10MPa, the temperature of extraction tower is 0 DEG C -250 DEG C.
Described quench oil is the oil distillate of oil scrubber tower reactor in ethylene unit chilling system, and its typical composition is many cyclophanes
Hydrocarbon, colloid, asphalitine.Described ethylene unit is mainly made up of the system such as industrial pyrolysis furnace and chilling, compression, separation, chilling
System mainly includes quencher, oil scrubber, water scrubber.
The method of the present invention can specifically use following technical scheme：
The Pintsch process gas that pyrolysis furnace 1 is exported (contains from H2Constituted to Pyrolysis fuel oil PFO etc., also comprising dilution steam generation), warp
Cross waste heat boiler to reclaim heat and enter quencher 2 after cooled, directly contact, cool down with quench oil.Cracking gas after cooling
Enter oil scrubber 3 together with quench oil, carry out Oil-gas Separation.The cracking gas that oil wash column overhead is drawn enters water scrubber 4 and moisture
From rear, various hydrocarbon products are separated into by compressibility 5 and piece-rate system 6.The circulation quench oil that oil scrubber tower reactor is drawn, enters
Enter Dilution steam generator 11, produce dilution steam generation.Carried by improving the bottom temperature mode of ethylene unit chilling system oil scrubber 3
High circulation chilling oil temperature, so as to improve the generating capacity of dilution steam generation.
It is divided into three tunnels after circulation quench oil is cooled, pyrolysis furnace quencher 2 is removed all the way；Pass through technique water preheater 12 all the way
Oil scrubber is returned again to, after being pressurizeed all the way by booster pump 10, into the quench oil charging aperture of extraction tower 7.
One decomposition under high pressure gas is drawn for solvent from ethylene unit compressibility, it is molten into the solvent feed mouthful of extraction tower 7
Agent and quench oil are implemented to extract in extraction tower 7, and obtained extract oil (solvent and the mixture of quench oil light component) is from extracting
The extracting oil export of top of tower is drawn, and the asphalt outlet of obtained raffinate pitch from extracting tower bottom is drawn.
Extract oil raises temperature after the reduction pressure of pressure-reducing valve 8 through heat exchanger 9, returns to oil scrubber 3, and reduction is overall anxious
Cold oil viscosity.
The present invention increases dilution steam generation steam exhaling amount by improving oil scrubber bottom temperature, is reduced by solvent extraction depitching
Chilling oil viscosity, and by the decomposition under high pressure gas that is come out using ethylene unit compressibility as solvent, compression power consumption is reduced, improve second
Alkene device heat recovery efficiency, reduces the energy consumption of ethylene unit.
Brief description of the drawings
The system schematic of Fig. 1 present invention
Description of reference numerals：
1 pyrolysis furnace, 2 quenchers, 3 oil scrubbers, 4 water scrubbers, 5 compressibilities, 6 piece-rate systems, 7 extraction towers, 8 pressure-reducing valves, 9
Preheater, 10 booster pumps, 11 Dilution steam generators, 12 preheaters.
Embodiment
With reference to embodiment, the present invention is further illustrated.
Embodiment：
Certain ethylene unit produces 200kt/a, year operation 8000h, ethylene yield 25t/h per year.Crack the Pintsch process of outlet of still
Gas (contains from H2Constituted to Pyrolysis fuel oil PFO etc., also comprising dilution steam generation), by waste heat boiler reclaim heat and it is cooled after,
Total amount is 147t/h, into quencher, directly contacts, cools down with quench oil.Cracking gas and quench oil after cooling enter together
Oil scrubber, carries out Oil-gas Separation, 200 DEG C of bottom temperature, tower reactor draws circulation quench oil, into Dilution steam generator, produces
Dilution steam generation 41t/h, circulation quench oil total amount is 1200t/h.It is divided into three tunnels after quench oil is cooled, pyrolysis furnace chilling is removed all the way
Device, returns again to oil scrubber by technique water preheater all the way, and 6t/h quench oil enters extraction tower quench oil charging aperture all the way, from
Compressibility draws one 6t/h cracking gas for solvent, by solvent extraction in extraction tower, is removed from extracting tower bottom to drip
Heavy constituent 1.5t/h based on green grass or young crops.Oil scrubber is returned after the extract oil decompression heating that extracting tower top is obtained, chilling oil viscosity is reduced
For 58.Ethylene unit energy consumption is 545GJ/h.
Comparative example
Certain ethylene unit produces 200kt, year operation 8000h, ethylene yield 25t/h per year, and chilling system charging total amount is 147t/
H, oil scrubber bottom draw circulation quench oil by Dilution steam generator produce dilution steam generation, then go pyrolysis furnace quencher to
Oil scrubber is returned after cracking gas cooling.Chilling oil viscosity 2000mm2/ s, consumes tempering oil 4t/h, and oil scrubber bottom temperature is 178
DEG C, generation dilution steam generation only has 12t/h, and ethylene unit energy consumption is 643GJ/h.
Claims (5)
1. a kind of method for reducing ethylene unit energy consumption, it is characterised in that the cracking gas of cracking outlet of still is cooled down through quencher
After send into oil scrubber, carry out material separation, quench oil drawn from oil scrubber bottom of towe, part quench oil is sent to quencher；Part is anxious
Cold oil returns to oil scrubber；Part quench oil enters extraction tower and carries out solvent extraction, and extraction tower tower top material returns to oil scrubber, extraction tower
Materials at bottom of tower pitch is mutually drawn, and wherein solvent used in extraction tower is the cracking gas that ethylene device compressor is exported, oil scrubber
Bottom temperature is 190-250 DEG C.
2. the method for ethylene unit energy consumption is reduced as claimed in claim 1, it is characterised in that oil scrubber bottom temperature is 195-
235℃。
3. the method for ethylene unit energy consumption is reduced as claimed in claim 1, it is characterised in that enter the solvent and urgency of extraction tower
The weight ratio of cold oil is 0.01-20.
4. the method for ethylene unit energy consumption is reduced as claimed in claim 3, it is characterised in that enter the solvent and urgency of extraction tower
The weight ratio of cold oil is 0.5-5.
5. the method for reduction ethylene unit energy consumption as claimed in claim 1, it is characterised in that the pressure of the extraction tower is
0.5MPa-10MPa, tower top temperature is 0 DEG C -250 DEG C.
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| CN111320525A (en) * | 2020-03-02 | 2020-06-23 | 大连理工大学 | Non-low temperature separation process for ethylene-rich catalytic cracking gas |
| CN114432844B (en) * | 2020-11-04 | 2023-05-12 | 中国石油化工股份有限公司 | Method and system for purifying pyrolysis gas |
| WO2022166740A1 (en) * | 2021-02-02 | 2022-08-11 | 中国石油化工股份有限公司 | Cracked gas heat recovery apparatus and cracked gas heat recovery method |
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| CN103305258A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
| CN103305259A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
| CN103305257A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
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| CN103305258A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
| CN103305259A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
| CN103305257A (en) * | 2012-03-16 | 2013-09-18 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
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