CN104449826A - Method for reducing ethylene unit quenching oil viscosity - Google Patents
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- CN104449826A CN104449826A CN201310419167.7A CN201310419167A CN104449826A CN 104449826 A CN104449826 A CN 104449826A CN 201310419167 A CN201310419167 A CN 201310419167A CN 104449826 A CN104449826 A CN 104449826A
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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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
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Abstract
The invention discloses a method for reducing ethylene unit quenching oil viscosity. The method comprises solvent-based extraction of quenching oil from an ethylene unit, and solvent recovery for viscosity-reduced quenching oil acquisition. A weight ratio of the solvent to the quenching oil in solvent-based extraction is 0.01-1.99 and preferably is 0.5-1.99. The method comprises the following steps of 1, solvent-based extraction: introducing quenching oil from an ethylene unit, carrying out solvent-based extraction in an extraction tower, separating extract oil from the tower top and separating raffinate asphalt from the top bottom, and 2, solvent recovery: carrying out heating and/or pressure reduction on the extract oil obtained by the step 1, feeding the extract oil into a solvent recovery tower and separating a solvent and viscosity-reduced quenching oil. The method greatly reduces ethylene unit quenching oil viscosity. The method utilizes a low solvent ratio in solvent extraction so that visbreaking effects are improved, a solvent circulation volume is greatly reduced and energy consumption is reduced.
Description
Technical field
The present invention relates to ethylene production field, furtherly, relate to a kind of method reducing ethylene unit quenching oil viscosity.
Background technology
At present, main ethylene unit adopts steam heat cracking technology to produce the basic organic chemical raw materials such as ethene, propylene, divinyl, aromatic hydrocarbons in the world.The raw materials such as lighter hydrocarbons, petroleum naphtha, hydrogenation tail oil and a certain proportion of dilution steam generation are blended in industrial pyrolysis furnace and scission reaction occur under hot conditions, and split product goes out the industrial chemicals such as ethene, propylene, divinyl through operation final production such as over-quenching, compression, separation.
Quenching system is an important component part of ethylene unit, is made up of, carries the task of separating and cracking gasoline, diesel oil, oil fuel component equipment such as quencher, oil scrubber, water wash columns, is also the key equipment reclaiming heat.As the first operation of cracking of ethylene gas disposal, it usually becomes the bottleneck of restriction ethylene unit output and running steady in a long-term, and it runs quality to ethylene unit performance important.
The splitting gas that the outlet of industrial pyrolysis furnace waste heat boiler comes is sent into bottom oil scrubber at quencher after quenching oil spraying cooling, and after reflux cooling, the heavy component in split product coagulates at the bottom of tower and is incorporated in quenching oil.Light constituent in split product, from oil scrubber Base top contact, enters water wash column and continues to be cooled to about 40 DEG C, enter follow-up compression separation system.Most of dilution steam generation required for cracking derives from the UTILIZATION OF VESIDUAL HEAT IN of device internal quench oil, and insufficient section is supplemented by pipe network steam.Oil wash column bottom temperature is higher, steam generation more, and it is better that device by utilizing waste heat utilizes, and outer benefit steam consumption is fewer.Therefore the height of oil wash column bottom temperature directly determines the size of waste heat recovery volume, also affects device production cost.In quenching system, quenching oil constantly circulates between quencher and oil wash tower reactor, and it is per hour that its internal circulating load often reaches a few kiloton, and the extraction of oil product only has tens tphs, causes quenching oil to be detained for a long time in system.Owing to containing the unsaturated aromatic hydrocarbon such as vinylbenzene, indenes component in split product quenching oil, the circulation under long high temperature of these materials can be polymerized, and generates macromolecular substance, causes quenching oil viscosity to increase, quenching oil moving situation is worsened, affects heat transfer effect.Owing to cannot improve by quenching oil viscosity influence oil wash column bottom temperature, cause quenching oil heat recuperation incomplete, cause dilution steam generation generating capacity wretched insufficiency, therefore need a large amount of steam to fill into system, cause energy dissipation.Simultaneously because quenching oil viscosity increases, add the power of systemic circulation pump, cause plant energy consumption to remain high.For this reason, ethene technical patent business applies various viscosity reducing technology to reduce quenching oil viscosity.
Traditional process for reducing viscosity adds modified thinning oil (Pyrolysis gas oil PGO) to reduce viscosity.Pyrolysis gas oil PGO blending in quenching oil, though the effect reducing quenching oil viscosity can be played, also Shortcomings part.First, the internal circulating load of Pyrolysis gas oil PGO in oil scrubber can be increased, strengthen the gas phase load in the middle part of oil scrubber tower reactor to tower, correspondingly reduce the processing power of oil scrubber; Secondly, containing a large amount of components such as vinylbenzene, naphthalene, indenes in Pyrolysis gas oil PGO, when they are along with quenching oil circulation time, polymkeric substance can be produced by polymerization reaction take place, and on the column plate accumulating in oil scrubber or filler, affect heat transfer and the mass transfer effect of column plate and filler, make tower pressure reduction increase, the processing power of tower declines; Again, due to the increase of Pyrolysis gas oil PGO internal circulating load, can component containing part diesel oil in the pyrolysis gasoline of tower top and the Pyrolysis fuel oil PFO of tower reactor extraction, have influence on the quality of pyrolysis gasoline and oil fuel, the operation of follow-up quenching water column time serious, can be made to worsen; Finally, because the amount of quenching oil is very large, therefore in order to reduce chilling oil viscosity, usually need to mix a large amount of Pyrolysis gas oil PGOs, and the time of injecting is longer, otherwise visbreaking effect is poor.
Viscosity depressant is that research department and ethene patent business worked out the chemical agent of various applicable reduction quenching oil viscosity both at home and abroad in recent years, suppresses the activity of polyreaction free radical to realize visbreaking target by adding chemical assistant.Chinese patent CN101062880A proposes a kind of quench oil viscosity reductant be made up of stopper, dispersion agent and metal passivator, there is the effect suppressing polymerization, prevent gathering and passivating metallic surfaces, reduce corrosion and the fouling of quenching system equipment, add-on is few, and there is satisfactory stability, the side effect of oil-water emulsion can not be produced.Add viscosity depressant and do not change quenching oil composition, fundamentally cannot solve quenching oil viscosity high problem.
Visbreaking tower visbreaking principle is, from the quenching oil of quenching oil circulation pump outlet, under the control of temperature control valve (TCV), the ethane cracking gas come with Control for Pyrolysis Furnace Area contacts in nozzle mixer, and the light constituent in quenching oil is vaporized, and enters visbreaking tower with splitting gas.Visbreaking tower is made up of two sections, and epimere is a cyclonic separator, and hypomere is a free-falling district.After mixture enters visbreaking tower, first in cyclonic separator, carry out the separation of liquid phase, the light constituent of vaporizing in ethane cracking gas and quenching oil enters oil scrubber tower reactor from visbreaking tower tower top, the heavy liquid phase component of not vaporizing passes through hypomere, enter visbreaking tower tower reactor, output to tank field as byproduct (Pyrolysis fuel oil PFO).Like this, from quenching oil, fractionate out the heavier feeds containing a large amount of resin and asphalt selectively and light material is stayed in systems in which, the light component concentration in quench oil circulated is increased, thus reducing quenching oil viscosity.Utilize ethane outlet of still splitting gas or directly use the steam stripped mode of steam heat, by the light constituent stripping in quenching oil is turned back in the recycle system, the oil that in the increase quenching oil recycle system, lightweight oil dilution proportion viscosity is high is utilized to realize visbreaking, to ensure system stable operation.
The weak point of the method is: one is that ethane stove must use high compressed steam air lift when burning, and gas phase directly returns quenching oil column, and quenching oil column load is high; Two is that to send light constituent content in heavy fuel oil after stripping outside less, sends pipeline outside and easily blocks.From the condition of production of each cover ethylene unit, only have part ethylene unit Reduce viscosity tower normal operation and reach certain visbreaking effect.Because visbreaking system cloud gray model is abnormal, there is larger gap in the actual motion index of most of device quench oil system and original design value, becomes the bottleneck of limit production ability.Adopt the steam stripped process for reducing viscosity of water vapor in actually operating because heavy fuel oil in fact all can not normally run in the blocking of visbreaking tower reactor.
The splitting gas that Chinese patent CN101074184 proposes pyrolyzer outlet comes is sent into bottom oil scrubber after cooling, carries out separating substances, forms three bursts of backflows; Quenching oil at the bottom of tower is after cooling, and part returns oil scrubber, and part is sent outside; Stage casing dish oil is after cooling, and part returns oil scrubber, and part is blended at the bottom of tower and is used as adjusting viscosity, and part is sent outside; Trim the top of column gasoline enters through pipeline, and pyrolyzer sends into rear system after carrying out logistics cooling the most at last.This method only optimizes oil scrubber temperature distribution, does not change quenching oil composition, little to the effect of reduction viscosity, and increases oil scrubber stage casing load, affects throughput.
Though aforesaid method partly can play the effect reducing quenching oil viscosity, the high problem of quenching oil viscosity fundamentally cannot be solved.It is reasonable not all to there is Reduce viscosity system design in current domestic a lot of ethylene unit, quenching oil viscosity is high, and quenching oil column tower top temperature is higher, bottom temperature is on the low side, and Reduce viscosity system cloud gray model is unstable, the problems such as heat recovery efficiency is low, quenched water emulsification often.Ensureing that quench oil system is made up of and operational condition the material be suitable for from technological design, will take innovative approach to irrational visbreaking technique, is the key point of guarantee system continuous and steady operation.
Summary of the invention
For solving produced problem in prior art, the invention provides a kind of method reducing ethylene unit quenching oil viscosity.Quenching oil obtains the quenching oil of visbreaking after solvent extraction and solvent recuperation, reduces the material consumption of visbreaking system while reducing quenching oil viscosity.
The object of this invention is to provide a kind of method reducing ethylene unit quenching oil viscosity.
Comprise:
Quenching oil from ethylene unit obtains visbreaking cold oil after solvent extraction and solvent recuperation;
In solvent extraction, the weight ratio of solvent and quenching oil is 0.01-1.99, is preferably 0.5-1.99.
Specifically comprise the following steps:
(1) solvent extraction: draw one quenching oil from ethylene unit, under extraction tower inner high voltage, implement solvent extraction, tower top isolates extract oil, isolates lighter pitch phase at the bottom of tower;
(2) solvent recuperation: the extract oil obtained from step (1), by heat up with or step-down after pass into solvent recovery tower and be separated and obtain solvent and visbreaking quenching oil; Solvent cycle uses, and visbreaking quenching oil returns ethylene unit, thus reduces quenching oil overall viscosity.
Wherein, described solvent is selected from one in C2-C6 alkane or alkene or its mixture, is preferably the one in C3-C5 alkane or its mixture.
In described solvent extraction, quenching oil feed temperature range is 30-230 DEG C, and solvent feed temperature range is 30-230 DEG C;
Described extraction tower pressure range is 1MPa-10MPa, and extraction tower temperature range is 30 DEG C-230 DEG C;
The pressure range of described solvent recovery tower is 0.1MPa-10Mpa; The temperature range of solvent recovery tower is 30 DEG C-300 DEG C;
Described quenching oil is the oil distillate of oil scrubber tower reactor in ethylene unit quenching system, and its typical composition is polycyclic aromatic hydrocarbons, colloid, bituminous matter.Described ethylene unit primarily of industrial pyrolysis furnace and chilling, compression, the System's composition such as to be separated, quenching system mainly comprises quencher, oil scrubber, water wash column.
Specifically can by the following technical solutions:
Solvent enters from the solvent feed mouth of extraction tower, enter from the quenching oil opening for feed of extraction tower after ethylene unit quenching system draws the pressurization of one quenching oil, solvent and quenching oil implement extracting in extraction tower, the extract oil obtained is drawn from the extract oil outlet at extraction tower top, and blue or green the outlet from the bituminous matter bottom extraction tower of the heeltap of taking out obtained is drawn.Extract oil reduces pressure through reducing valve, because throttling expansion operative temperature declines, then heater via heating, enter solvent recovery tower import after raised temperature.Take out that the heeltap is blue or green to be reduced after pressure as pitch or fuel oil products extraction by reducing valve.
Extract oil is separated into solvent and visbreaking quenching oil in solvent recovery tower, and visbreaking quenching oil is drawn at the bottom of tower, and solvent is drawn from tower top.The solvent of drawing from solvent recovery tower enters solvent cycle compressor increase pressure, and simultaneous temperature raises.The solvent of high temperature is through condenser condenses, and after mixing in mixing tank with supplementing solvent, the solvent again as extraction tower enters extraction tower solvent feed mouth.
After the temperature and pressure close with ethylene unit quenching oil adjusted to by the visbreaking quenching oil of solvent recovery tower extraction, return quenching system, thus reduce overall quenching oil viscosity.
The present invention is a kind of solvent extraction method reducing ethylene unit quenching oil viscosity, by carrying out solvent extraction process to ethylene unit quenching oil, remove bituminous matter wherein, the quenching oil of visbreaking is obtained again through solvent recovery step, this low viscous visbreaking oil is returned quenching system oil scrubber, significantly can reduce ethylene unit chilling oil viscosity thus.Owing to have employed lower solvent ratio in solvent extraction, while raising visbreaking effect, greatly reduce solvent cycle amount, reduce energy consumption.
Accompanying drawing explanation
Fig. 1 method schematic diagram of the present invention
Description of reference numerals:
1 extraction tower, 2 reducing valve A, 3 reducing valve B, 4 process furnace, 5 solvent recovery towers, 6 water coolers, 7 solvent cycle compressors, 8 condensers, 9 mixing tanks.
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
11008mPa.s when chilling oil viscosity used is normal pressure 50 DEG C in embodiment, quenching oil mid-boiling point accounts for 33% of gross weight higher than the component of 629 DEG C.
Embodiment 1:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with propane.Quenching oil feeding temperature is 90 DEG C, and pressure is 10MPa, flow 10t/h.Solvent feed temperature is 90 DEG C, and pressure is 10MPa, flow 19t/h, and solvent and quenching oil weight ratio are 1.9.The solvent of quenching oil and its weight 0.05 times enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 90 DEG C, and pressure is 10MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.8MPa normal pressure desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.8MPa, after adjustment temperature to 90 DEG C, sends in the middle part of solvent recovery tower.Solvent recovery tower is void tower, this pressure tower 0.8MPa, and in tower, uniformity of temperature profile is 90 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 10MPa and recycle.Obtain visbreaking quenching oil 4229kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 14.3mPa.s.
Embodiment 2:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with propane.Quenching oil feeding temperature is 70 DEG C, and pressure is 5MPa, flow 10t/h.Solvent feed temperature is 70 DEG C, and pressure is 5MPa, flow 10t/h, and solvent and quenching oil weight ratio are 1.The solvent of quenching oil and its weight 0.05 times enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 70 DEG C, and pressure is 5MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.8MPa normal pressure desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.8MPa, after adjustment temperature to 70 DEG C, sends in the middle part of solvent recovery tower.Solvent recovery tower is void tower, this pressure tower 0.8MPa, and in tower, uniformity of temperature profile is 70 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 5MPa and recycle.Obtain visbreaking quenching oil 3616kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 6.7mPa.s.
Embodiment 3:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with propane.Quenching oil feeding temperature is 30 DEG C, and pressure is 5MPa, flow 10t/h.Solvent feed temperature is 30 DEG C, and pressure is 5MPa, flow 5t/h, and total solvent and quenching oil weight ratio are 0.5.The solvent of quenching oil and its weight 0.05 times enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 30 DEG C, and pressure is 5MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.5MPa desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.5MPa, and after adjustment temperature to 30 DEG C, send in the middle part of solvent recovery tower, this pressure tower 0.5MPa, in tower, uniformity of temperature profile is 30 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 5MPa and recycle.Obtain visbreaking quenching oil 3750kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 4.0mPa.s.
Embodiment 4:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with normal butane.Quenching oil feeding temperature is 90 DEG C, and pressure is 10MPa, flow 10t/h.Solvent feed temperature is 90 DEG C, and pressure is 10MPa, flow 19t/h, and solvent and quenching oil weight ratio are 1.9.The solvent of quenching oil and its weight 0.05 enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 90 DEG C, and pressure is 10MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.8MPa normal pressure desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.8MPa, after adjustment temperature to 90 DEG C, sends in the middle part of solvent recovery tower.Solvent recovery tower is void tower, this pressure tower 0.8MPa, and in tower, uniformity of temperature profile is 90 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 10MPa and recycle.Obtain visbreaking quenching oil 5646kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 28.7mPa.s.
Embodiment 5:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with normal butane.Quenching oil feeding temperature is 90 DEG C, and pressure is 4MPa, flow 10t/h.Solvent feed temperature is 90 DEG C, and pressure is 4MPa, flow 19.9t/h, and solvent and quenching oil weight ratio are 1.99.The solvent of quenching oil and its weight 0.05 times enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 90 DEG C, and pressure is 4MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.8MPa normal pressure desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.8MPa, after adjustment temperature to 90 DEG C, sends in the middle part of solvent recovery tower.Solvent recovery tower is void tower, this pressure tower 0.8MPa, and in tower, uniformity of temperature profile is 90 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 4MPa and recycle.Obtain visbreaking quenching oil 5937kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 18.3mPa.s.
Embodiment 6:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with Trimethylmethane.Quenching oil feeding temperature is 120 DEG C, and pressure is 4MPa, flow 10t/h.Solvent feed temperature is 120 DEG C, and pressure is 4MPa, flow 5t/h, and solvent and quenching oil weight ratio are 0.5.The solvent of quenching oil and its weight 0.05 times enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 120 DEG C, and pressure is 4MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.8MPa normal pressure desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.8MPa, after adjustment temperature to 120 DEG C, sends in the middle part of solvent recovery tower.Solvent recovery tower is void tower, this pressure tower 0.8MPa, and in tower, uniformity of temperature profile is 120 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 4MPa and recycle.Obtain visbreaking quenching oil 2858kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 18.9mPa.s.
Embodiment 7:
Be that solvent carries out the process of solvent extraction visbreaking to quenching oil with propane.Quenching oil feeding temperature is 70 DEG C, and pressure is 5MPa, flow 10t/h.Solvent feed temperature is 70 DEG C, and pressure is 5MPa, flow 10t/h, and solvent and quenching oil weight ratio are 1.The solvent of quenching oil and its weight 0.05 enters from extraction tower top, and remaining solvent is entered by extraction tower bottom.Extraction tower temperature is 70 DEG C, and pressure is 5MPa.Extraction tower tower top isolates extract oil, isolates and take out heeltap green grass or young crops at the bottom of tower.After pitch is depressurized to 0.8MPa normal pressure desolvation mutually, as oil fuel extraction.
The extract oil that extraction tower tower top flows out is depressurized to 0.8MPa, after adjustment temperature to 90 DEG C, sends in the middle part of solvent recovery tower.Solvent recovery tower is void tower, this pressure tower 0.8MPa, and in tower, uniformity of temperature profile is 70 DEG C.Now solvent is declined to a great extent by density, and dissolving power declines, thus realizes solvent and visbreaking chilling oil separating.Obtain solvent from solvent recuperation column overhead, and be pressurized to 5MPa and adjust to 70 DEG C of Posterior circle and use.Obtain visbreaking quenching oil 3546kg/h from solvent recovery tower tower reactor, during normal pressure 50 DEG C, viscosity is 9.7mPa.s.
Comparative example:
Existing visbreaking tower technique is for draw one quenching oil from the ethylene unit quenching oil recycle system, and its temperature is 195 DEG C, and pressure is 0.16MPa.Ethane stove splitting gas temperature is 500 DEG C, and pressure is 0.16MPa.This quenching oil and ethane stove splitting gas are mixed into visbreaking tower, and visbreaking tower pressure is 0.16MPa, and temperature is 272 DEG C, and tower top is separated and obtains visbreaking quenching oil, isolates heavy fuel oil at the bottom of tower.(viscosity is 65mm to the visbreaking quenching oil of 272 DEG C
2/ s) enter oil scrubber bottom.Existing method have lost the higher-grade heat energy of ethane stove splitting gas, is also taken in quenching system.
Claims (7)
1. reduce a method for ethylene unit quenching oil viscosity, it is characterized in that described method comprises:
Quenching oil from ethylene unit obtains visbreaking quenching oil after solvent extraction and solvent recuperation;
In solvent extraction, the weight ratio of solvent and quenching oil is 0.01-1.99.
2. the method reducing ethylene unit quenching oil viscosity as claimed in claim 1, is characterized in that:
In solvent extraction, the weight ratio of solvent and quenching oil is 0.5-1.99.
3. the method reducing ethylene unit quenching oil viscosity as claimed in claim 1, is characterized in that described method comprises:
(1) solvent extraction: draw one quenching oil from ethylene unit, implement solvent extraction in extraction tower, tower top isolates extract oil, isolates at the bottom of tower and takes out heeltap green grass or young crops;
(2) solvent recuperation: the extract oil obtained from step (1), obtains solvent and visbreaking quenching oil by heating up and/or passing into solvent recovery tower separation after step-down.
4. the method reducing ethylene unit quenching oil viscosity as claimed in claim 1, is characterized in that:
Described solvent is selected from one in C2-C6 alkane or alkene or its mixture.
5. the method reducing ethylene unit quenching oil viscosity as claimed in claim 4, is characterized in that:
Described solvent is one in C3-C5 alkane or its mixture.
6. the method reducing ethylene unit quenching oil viscosity as claimed in claim 1, is characterized in that:
In described solvent extraction, quenching oil feeding temperature is 30-230 DEG C, and solvent feed temperature is 30-230 DEG C.
7. the method reducing ethylene unit quenching oil viscosity as claimed in claim 2, is characterized in that:
Described extraction tower pressure is 1MPa-10MPa, and the temperature of extraction tower is 30 DEG C-230 DEG C;
The pressure of described solvent recovery tower is 0.1MPa-10Mpa; The temperature range of solvent recovery tower is 30 DEG C-300 DEG C.
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| CN115477958A (en) * | 2021-06-16 | 2022-12-16 | 中国石油化工股份有限公司 | Quenching oil viscosity reducing system and method |
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| CN101962565A (en) * | 2010-10-19 | 2011-02-02 | 惠生工程（中国）有限公司 | Quench oil viscosity reducing process for two quench oil systems |
| CN102220169A (en) * | 2011-05-10 | 2011-10-19 | 沈阳石蜡化工有限公司 | Pyrolysis gas quenching structural unit of CPP (Catalytic Pyrolysis Production) and process thereof |
| CN102408925A (en) * | 2011-10-08 | 2012-04-11 | 中国石油化工股份有限公司 | High aromatic low-viscosity quenching and tempering oil for ethylene device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101962565A (en) * | 2010-10-19 | 2011-02-02 | 惠生工程（中国）有限公司 | Quench oil viscosity reducing process for two quench oil systems |
| CN102220169A (en) * | 2011-05-10 | 2011-10-19 | 沈阳石蜡化工有限公司 | Pyrolysis gas quenching structural unit of CPP (Catalytic Pyrolysis Production) and process thereof |
| CN102408925A (en) * | 2011-10-08 | 2012-04-11 | 中国石油化工股份有限公司 | High aromatic low-viscosity quenching and tempering oil for ethylene device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115477958A (en) * | 2021-06-16 | 2022-12-16 | 中国石油化工股份有限公司 | Quenching oil viscosity reducing system and method |
| CN115477958B (en) * | 2021-06-16 | 2024-03-19 | 中国石油化工股份有限公司 | Quenching oil viscosity reducing system and method |
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