CN101962565B - Quench oil viscosity reducing process for two quench oil systems - Google Patents
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Abstract
The invention relates to a quench oil viscosity reducing process for two quench oil systems. The process breakthroughs the conventional process of one quench oil system and one viscosity reducing tower by using the viscosity reducing technology of a viscosity reducing tower, and the quench oil viscosity control of two quench oil systems is realized at the same time under the condition of only arranging one ethane furnace and one viscosity reducing tower by using the quench oil intercommunication mode of the two quench oil systems. compared with the prior art, the process has the advantages of simple flow, low equipment investment and simple operation, the temperatures of the two quench oil systems are increased at the same time, the energy consumption of the device is greatly reduced, and the sewage discharge of the process is reduced.
Description
Technical field
The present invention relates to a kind of preparing ethylene by steam cracking technique, especially relate to a kind of technique of two cover quench oil system Reduce viscosities.
Background technology
The quenching system of ethylene unit is between Control for Pyrolysis Furnace Area and the compression disengaging zone, cracking stock utilizes the steam heat cracking technique to produce splitting gas by pyrolyzer, be sent to quenching system behind the Pintsch process gas process waste heat boiler recovery part heat that generates, the effect of quench oil system is: (1) further reclaims the entrained heat of splitting gas, and splitting gas is cooled to suitable temperature; (2) isolate oil fuel component the splitting gas from quench oil system.Deliver to again the compression disengaging zone through the splitting gas of quenching system and further separate, obtain different product (ethene, propylene etc.).Quenching system is in the junction of forming a connecting link in whole ethylene unit, the effect of its running and stability are to the ethylene unit important.
The dilution steam generation that the required steam of pyrolyzer thermo-cracking mainly produces from quench oil system, cracking stock situation according to China's ethylene unit, under design point, the ratio that the dilution steam generation amount that quenching oil occurs accounts for the needed total dilution steam generation amount of cracking is about about 55%～60%, and insufficient section needs indirectly and directly to replenish with middle pressure steam.Be lower than design temperature if quenching oil advances the temperature of Dilution steam generator, and the pressure and temperature of dilution steam generation there be fixing the requirement, so just cause heat transfer temperature difference to reduce; If the chilling oil viscosity is higher than design load, heat transfer coefficient is descended; This all can make quenching oil generation dilution steam generation amount reduce, and the middle pressure steam amount of replenishing increases, thereby increases the energy consumption of device.
China has the quench oil system of many cover ethylene units to have the running difficulty, quenching oil viscosity height becomes outstanding problem wherein, some installs quenching oil viscosity number even reaches more than the 4000mm2/s, had a strong impact on the steady running of device, too high in order to prevent quenching oil viscosity, these devices have to reduce quenching oil tower reactor temperature, cause quenching oil dilution steam generation generating capacity few, the middle pressure steam that fills into is many, and the comprehensive energy consumption of ethene is high, and the process spent water of discharging simultaneously is many.Some device injects a large amount of tempering oils in quenching oil, additionally increased the running cost of device.
The Growth Mechanism of quenching oil viscosity there was in depth research both at home and abroad, research generally believes the increase of quenching oil viscosity mainly because the condensed-nuclei aromatics condensation causes the molecule increase to cause, so condensed-nuclei aromatics concentration in quenching oil is larger, just easier condensation causes quenching oil viscosity to raise.The key of visbreaking is exactly to adjust quenching oil to form, and reduces the content of condensed-nuclei aromatics in quenching oil, increases the content of the intermediate component of " high boiling point, low viscosity ".At present domestic ethylene has adopted different means and technology for control quenching oil viscosity, and common methods has in quenching oil and adds viscosity depressant, adding tempering oil, is exactly Viscosity Decrease Technology in addition.Add viscosity depressant and can not change the chilling oil composition, just suppressed the autohemagglutination that restructuring divides in the quenching oil, can not tackle the problem at its root; Add tempering oil and can change the chilling oil composition, but the tempering oil quality that adds is had particular requirement, add-on is larger simultaneously, the low viscosity of guarantee quenching oil and high-temperature, and this method has improved the production cost of device greatly; Viscosity Decrease Technology is technology relatively more commonly used in the present Research On Decreasing Viscosity of Quench Oil, they are different according to technical process and stripping medium, can be divided into again vacuum extraction technology, steam stripped technology, splitting gas steam stripping technique etc., that the vacuum extraction technology is used at home is less (has two cover ethylene units to adopt, only have at present and one be enclosed within usefulness), the steam stripped technology is widely used in early days, but stripping and visbreaking effect are not very desirable, ethane stove splitting gas steam stripping technique is satisfactory for result to stripping and the visbreaking of quenching oil, is recommendable technology.The Viscosity Decrease Technology advantage is to utilize the material of self and technical process to reach suitable or desirable quenching oil composition distribution.If the quenching oil component be divided into simply L (gently), M (in) and H (weight) component, wherein the M component comprises high boiling point, low viscosity component, the H component comprises the restructuring such as condensed-nuclei aromatics minute, Viscosity Decrease Technology then is quenching oil to be fractionated out gently, neutralize to recombinate selectively divide, stripping goes out suitable ingredients and turns back in the quenching oil column, reaches the purpose that reduces quenching oil viscosity with this.
At present domestic many cover ethylene units have two cover quench oil system, and according to the difference of cracking stock, there are the problems such as the high and quenching oil tower reactor temperature of quenching oil viscosity is low in two cover quench oil system, are threatening the steady running of ethylene unit and are limiting saving energy and reduce the cost of installing.Be proved to be advanced person's Research On Decreasing Viscosity of Quench Oil as the visbreaking tower technology of stripping medium with ethane stove splitting gas.But for two cover quench oil system in the same ethylene unit, because the control of ethane feed quantitative limitation and cost of investment, ethane cracking furnace is set separately and the visbreaking tower can not or be not easy realization in every cover quench oil system.So the technical process that " realizes two cover quench oil system visbreakings with visbreaking tower " arranges separately the ethane stove with two cover quench oil system and compares with the technical process of visbreaking tower, the former flow process and simple to operate, facility investment is few.And the effect that can reach equally visbreaking and save energy and reduce the cost.
Summary of the invention
Purpose of the present invention is exactly to provide a kind of improvement technique for the defective that overcomes above-mentioned prior art existence.
Purpose of the present invention can be achieved through the following technical solutions:
A kind of technique of two cover quench oil system Reduce viscosities, include two cover quench oil system, it is characterized in that, this technique is at the newly-increased visbreaking tower of first set quench oil system, increase or transform a pyrolyzer newly in the corresponding Control for Pyrolysis Furnace Area of first set quench oil system, the quenching oil of the second cover quench oil system quenching oil column tower reactor is sent in the pyrolyzer and is mixed with splitting gas, the gas-oil mixture that obtains is sent into the visbreaking tower of first set quench oil system, the visbreaking top gaseous phase is admitted to first set quenching system quenching oil tower reactor, visbreaking tower reactor liquid phase is divided into three strands, one is got back to the visbreaking tower reactor and forms self circulation, another thigh is delivered to first set quenching oil column tower reactor, remaining one delivered to the tank field as product, and the quenching oil of first set quenching oil column tower reactor is sent the second cover quenching oil column tower reactor back to and kept the second cover quenching oil column tower reactor liquid level.
Described pyrolyzer is ethane cracking furnace or ethane and Deposition During Propane Pyrolysis stove.
The single loop circulation between two quenching oil columns of described visbreaking tower and quenching oil reaches the purpose of two cover quench oil system Reduce viscosities, be that first set quench oil system part quenching oil is sent to the second cover quench oil system, the second cover quench oil system part quenching oil returns again the first set quench oil system through the visbreaking tower, realizes balance and the steady running of two cover quench oil system.
Compared with prior art, the present invention had both considered that ethane or " ethane+propane " stove splitting gas were as the advantage of stripping medium, also considered the cost control in the quantitative limitation of ethane stove raw material and the investment, the present invention arranges an ethane or " ethane+propane " stove and a visbreaking tower in two cover quench oil system, adopt ethane stove splitting gas as the stripping medium, mode by two cover quenching oils are gone here and there mutually can effectively reduce quenching oil viscosity, improves quenching oil tower reactor temperature.When same ethylene unit has two cover quench oil system, often there is the corresponding pyrolyzer cracking stock of a cover quenching system heavier, quenching oil viscosity is very high, the corresponding pyrolyzer cracking stock of another set of quenching system is lighter, quenching oil tower reactor temperature is lower, perhaps two cover quenching system cracking stocks are all heavier, mode by the circulation of quenching oil single loop, at first can balance because the cracking stock weight causes the difference of two cover quenching system splitting gases restructuring components, can make the quenching oil of two cover quenching systems form more approaching, secondly pass through the visbreaking of a visbreaking tower, just can guarantee that two cover quench oil system quenching oil viscosity reduce simultaneously, can make the temperature of two cover quenching oil tower reactors be improved simultaneously at last.
Use the content that the present invention can improve " high boiling point, low viscosity " component in the two cover quench oil system quenching oils simultaneously, for main ethylene unit take petroleum naphtha as cracking stock, quenching oil tower reactor temperature is brought up to more than 195 ℃, can be along with 1 ℃ of 1-2t/h that mostly occurs of the every rising of quenching oil tower reactor temperature to the dilution steam generation amount that the ethylene unit quenching oil more than 300,000 t/a occurs, inject in the tempering oil situation stopping simultaneously, viscosity controller is in 300mm2/s.Use the operation stability that the present invention can improve device, reduce the running cost of device, most importantly can significantly reduce the energy expenditure of device, reduce the process spent water quantity discharged.
Description of drawings
Fig. 1 is the common technology general flow chart of two cover quench oil system;
Fig. 2 is the common technology general flow chart of two cover quench oil system after improving;
Fig. 3 is process flow diagram of the present invention.
Embodiment
The present invention is described in detail below in conjunction with the drawings and specific embodiments.
Embodiment
Take the ethylene unit of 600,000 ton/years of throughput as example, old device quenching system processing power is 330,000 ton/years, the corresponding cracking stock of splitting gas is heavy hydrocarbon (about 72%) and petroleum naphtha (about 28%), new device quenching system processing power is 270,000 ton/years, and cracking stock is hydrogenation tail oil (about 20%) and petroleum naphtha (about 80%).Flow process shown in Figure 3 is adopted in technical process.Major equipment comprises quenching oil column 34,323; Quenching oil circulation pump 37,324; Dilution steam generator 36,325; Visbreaking tower 32; Visbreaking tower reactor liquid pump 33; Middle oily heat exchange user 35,326; The pipeline 38～322 of oil quencher 31 and old device, the pipeline 327～335 of new device.
Technical process is as follows:
The splitting gas that old device Control for Pyrolysis Furnace Area is come enters old device quenching oil column 34 through pipeline 320, the tower reactor quenching oil is carried by old device chilling oil pump 7 through pipeline 315 and is removed always to install Dilution steam generator 36 in order to dilution steam generation to occur, quenching oil is divided into two portions after the heat exchange, one large stock-traders' know-how pipeline 316 is got back to old device quenching oil column 34, a small gangs of removes new device quenching oil column 323 through pipeline 317, ethane stove splitting gas enters ethane furnace oil quencher 31 and mixes through the quenching oil of pipeline 335 from new device quenching oil column 323 tower reactors through pipeline 38, mixing enters visbreaking tower 32 by pipeline 321 tangent lines, visbreaking tower 32 top gaseous phases turn back to old device quenching oil column 34 through pipeline 314, the tower reactor liquid phase is divided into three strands through pipeline 322 by visbreaking tower reactor liquid pump 33, one stock-traders' know-how pipeline 312 turns back to visbreaking tower 32 bottoms, one stock-traders' know-how pipeline 313 turns back to old device quenching oil column 34, one is old through pipeline 311 conducts in addition, the total cracking heavy fuel oil of new device product is sent, the quenching oil and the splitting gas that turn back to old device quenching oil column 34 through pipeline 316 mix in tower, splitting gas after the cooling continues to rise to the tower middle part in that old device quenching oil column 34 is interior, oil is got back to tower middle and upper part by a series of middle oil heat exchanger users 35 by pipeline 319 through pipeline 318 from extract out at the tower middle part, with the splitting gas heat exchange of rising, splitting gas is further lowered the temperature, splitting gas moves on to top of tower on continuing, cat head gasoline refluxes and delivers to old device quenching oil column 34 tops through pipeline 39, and splitting gas is continued cooling and removes always to install quenching water column by pipeline 310.
The splitting gas that the new device Control for Pyrolysis Furnace Area is come enters new device quenching oil column 323 through pipeline 327, the tower reactor quenching oil is carried by new device chilling oil pump 324 through pipeline 333 and is divided into two strands, one large stock-traders' know-how pipeline 334 goes new device Dilution steam generator 325 in order to dilution steam generation to occur, a small gangs of removes ethane furnace oil quencher 31 through pipeline 335, quenching oil after 325 heat exchange of new device Dilution steam generator turns back to new device quenching oil column 323 through pipeline 328, mix in tower with splitting gas, splitting gas after the cooling continues to rise to the tower middle part in that new device quenching oil column 323 is interior, oil is got back to tower middle and upper part by a series of middle oil heat exchanger users 326 by pipeline 330 through pipeline 329 from extract out at the tower middle part, with the splitting gas heat exchange of rising, splitting gas is further lowered the temperature, cracker moves on to top of tower on continuing, cat head gasoline refluxes and delivers to new device quenching oil column 323 tops through pipeline 331, and splitting gas is continued cooling and removes the new device quenching water column by pipeline 332.
Ethane stove splitting gas flow 20.8t/h (comprising dilution steam generation), temperature is 515 ℃, old device splitting gas flow is 150t/h, old other stove splitting gas feeding temperature of device is 340 ℃, old device cat head gasoline quantity of reflux is 115t/h, new device splitting gas flow is 166t/h, new device splitting gas feeding temperature is 410 ℃, new device cat head gasoline quantity of reflux is 86t/h, the quenching oil flow that new device removes always to install ethane furnace oil quencher is 50t/h, visbreaking cat head service temperature is controlled at 256 ℃, and always installing the flow that quenching oil turns back to the new device quenching oil column is 47t/h.
Comparative Examples
Adopt flow process shown in Figure 1.11 is old device visbreaking tower among the figure, 12 is old device visbreaking tower reactor liquid pump, 13 is old device quenching oil column, 14 is oily hot user in the old device, 15 is old device Dilution steam generator, 16 is old device chilling oil pump, 17～119 is old device pipeline, 120 is new device visbreaking tower, 121 is new device visbreaking tower reactor liquid pump, 122 is the new device quenching oil column, 123 is oily hot user in the new device, 124 is the new device Dilution steam generator, 125 is new device chilling oil pump, 126～138 is the new device pipeline.
The splitting gas that old device Control for Pyrolysis Furnace Area is come enters old device quenching oil column 13 through pipeline 119, the tower reactor quenching oil is carried by old device chilling oil pump 16 through pipeline 112 and is divided into two strands, one large stock-traders' know-how pipeline 113 removes always to install Dilution steam generator 15 in order to dilution steam generation to occur, a small gangs of removes always to install visbreaking tower 11 through pipeline 114, steam enters old device visbreaking tower 11 stripping quenching oils through pipeline 18, old device visbreaking tower 11 top gaseous phases turn back to old device quenching oil column 13 through pipeline 117, the tower reactor liquid phase is sent as old device cracking heavy fuel oil product through pipeline 17 by old device visbreaking tower reactor liquid pump 12 through pipeline 116 again, quenching oil after old device Dilution steam generator 15 heat exchange turns back to old device quenching oil column 13 through pipeline 115, mix in tower with splitting gas, splitting gas after the cooling continues to rise to the tower middle part in that old device quenching oil column 13 is interior, oil is got back to tower middle and upper part by a series of middle oil heat exchanger users 14 by pipeline 119 through pipeline 118 from extract out at the tower middle part, with the splitting gas heat exchange of rising, splitting gas is further lowered the temperature, cracker moves on to top of tower on continuing, cat head gasoline refluxes and delivers to old device quenching oil column 13 tops through pipeline 110, and splitting gas is continued cooling and removes always to install quenching water column by pipeline 111.
The flow process of new device is the same with old device flow process.The splitting gas that the new device Control for Pyrolysis Furnace Area is come enters new device quenching oil column 122 through pipeline 128, the tower reactor quenching oil is carried by new device chilling oil pump 125 through pipeline 132 and is divided into two strands, one large stock-traders' know-how pipeline 133 goes new device Dilution steam generator 124 in order to dilution steam generation to occur, a small gangs of removes new device visbreaking tower 120 through pipeline 131, steam enters new device visbreaking tower 120 stripping quenching oils through pipeline 130, new device visbreaking tower 120 top gaseous phases turn back to new device quenching oil column 122 through pipeline 129, the tower reactor liquid phase is sent as new device cracking heavy fuel oil product through pipeline 138 by new device visbreaking tower reactor liquid pump 121 through pipeline 137 again, quenching oil after 124 heat exchange of new device Dilution steam generator turns back to new device quenching oil column 122 through pipeline 134, mix in tower with splitting gas, splitting gas after the cooling continues to rise to the tower middle part in that new device quenching oil column 122 is interior, oil is got back to tower middle and upper part by a series of middle oil heat exchanger users 123 by pipeline 136 through pipeline 135 from extract out at the tower middle part, with the splitting gas heat exchange of rising, splitting gas is further lowered the temperature, cracker moves on to top of tower on continuing, cat head gasoline refluxes and delivers to new device quenching oil column 122 tops through pipeline 127, and splitting gas is continued cooling and removes the new device quenching water column by pipeline 126.
Old device splitting gas flow is 176t/h, old other stove splitting gas feeding temperature of device is 340 ℃, old device cat head gasoline quantity of reflux is 160t/h, new device splitting gas flow is 166t/h, new device splitting gas feeding temperature is 410 ℃, new device cat head gasoline quantity of reflux is 92t/h, and the old and new's device stripped vapor consumption is 1t/h.
Because the steam stripped effect is limited, so effective stripping of failing goes out the useful component in the quenching oil, the visbreaking effect of quenching oil is undesirable, and quenching oil viscosity is higher, and quenching oil tower reactor temperature is often lower.
Ethane stove splitting gas can effectively solve the problem of stripping medium heat quantity not sufficient, and ethane stove splitting gas restructuring minute content is few, the pyrolysis furnace charring cycle is long, so ethane stove splitting gas is suitable quenching oil stripping medium, domestic Reduce viscosity transformation is adopted with the visbreaking tower technology flow process of ethane stove splitting gas as the stripping medium more.For the ethylene unit that two cover quenching systems are arranged, can adopt the technical process (omitting thin fuel oil stripping tower system and oil quencher among the figure) of Fig. 2,21 is old device ethane furnace oil quencher among the figure, 22 is old device visbreaking tower, 23 is old device visbreaking tower reactor liquid pump, 24 is old device quenching oil column, 25 is oily hot user in the old device, 26 is old device Dilution steam generator, 27 is old device chilling oil pump, 28～223 is old device pipeline, 224 is new device visbreaking tower, 225 is new device visbreaking tower reactor liquid pump, 226 is the new device quenching oil column, 227 is oily hot user in the new device, 228 is the new device Dilution steam generator, 229 is new device chilling oil pump, 230 is new device ethane furnace oil quencher, 231～246 is the new device pipeline.
The splitting gas that old device Control for Pyrolysis Furnace Area is come enters old device quenching oil column 24 through pipeline 223, the tower reactor quenching oil is divided into two portions through pipeline 217 by old device chilling oil pump 27, most is carried through pipeline 219 and removes always to install Dilution steam generator 26 in order to dilution steam generation to occur, quenching oil after the heat exchange is got back to old device quenching oil column 24 through pipeline 218, sub-fraction is removed always to install ethane furnace oil quencher 21 and is mixed through the old device ethane stove splitting gas of pipeline 28 through pipeline 220, mixed liquid phase enters old device visbreaking tower 22 through pipeline 216 tangent lines, old device visbreaking tower 22 top gaseous phases turn back to old device quenching oil column 24 through pipeline 214, the tower reactor liquid phase is divided into three strands through pipeline 215 by old device visbreaking tower reactor liquid pump 23, one stock-traders' know-how pipeline 212 turns back to old device visbreaking tower 22 bottoms, one stock-traders' know-how pipeline 213 turns back to old device quenching oil column 24, one is sent as old device cracking heavy fuel oil product through pipeline 211 in addition, the quenching oil and the splitting gas that turn back to old device quenching oil column 24 through pipeline 218 mix in tower, splitting gas after the cooling continues to rise to the tower middle part in that old device quenching oil column 24 is interior, oil is got back to tower middle and upper part by a series of middle oil heat exchanger users 25 by pipeline 222 through pipeline 221 from extract out at the tower middle part, with the splitting gas heat exchange of rising, splitting gas is further lowered the temperature, cracker moves on to top of tower on continuing, cat head gasoline refluxes and delivers to old device quenching oil column 24 tops through pipeline 29, and splitting gas is continued cooling and removes always to install quenching water column by pipeline 210.
The splitting gas that the new device Control for Pyrolysis Furnace Area is come enters new device quenching oil column 226 through pipeline 242, the tower reactor quenching oil is divided into two portions through pipeline 245 by new device chilling oil pump 229, most is carried through pipeline 231 and goes new device Dilution steam generator 228 in order to dilution steam generation to occur, quenching oil after the heat exchange is got back to new device quenching oil column 226 through pipeline 233, sub-fraction is removed new device ethane furnace oil quencher 230 and is mixed through the new device ethane stove splitting gas of pipeline 240 through pipeline 232, mixed liquid phase enters new device visbreaking tower 224 through pipeline 246 tangent lines, new device visbreaking tower 224 top gaseous phases turn back to new device quenching oil column 226 through pipeline 241, the tower reactor liquid phase is divided into three strands through pipeline 236 by new device visbreaking tower reactor liquid pump 225, one stock-traders' know-how pipeline 237 turns back to new device visbreaking tower 224 bottoms, one stock-traders' know-how pipeline 238 turns back to new device quenching oil column 226, one is sent as new device cracking heavy fuel oil product through pipeline 239 in addition, the quenching oil and the splitting gas that turn back to new device quenching oil column 226 through pipeline 233 mix in tower, splitting gas after the cooling continues to rise to the tower middle part in that new device quenching oil column 226 is interior, oil is got back to tower middle and upper part by a series of middle oil heat exchanger users 227 by pipeline 235 through pipeline 234 from extract out at the tower middle part, with the splitting gas heat exchange of rising, splitting gas is further lowered the temperature, cracker moves on to top of tower on continuing, cat head gasoline refluxes and delivers to new device quenching oil column 226 tops through pipeline 243, and splitting gas is continued cooling and removes the new device quenching water column by pipeline 244.
This process characteristic is that old device and new device operate separately, all use ethane stove splitting gas as the stripping medium of quenching oil, need to an ethane stove and visbreaking tower respectively be set at old device and new device, the equipment that also has pump, strainer etc. to match, because the restriction that ethane stove cracking stock amount is limited and the control of cost of investment, this flow process often can not realize or be uneconomical.
Utilize technical process and the treatment effect among the embodiment of Fig. 1 more as shown in table 1.
Table 1
Claims (3)
1. the technique of a cover quench oil system Reduce viscosity, include two cover quench oil system, it is characterized in that, this technique is at the newly-increased visbreaking tower of first set quench oil system, increase or transform a pyrolyzer newly in the corresponding Control for Pyrolysis Furnace Area of first set quench oil system, the quenching oil of the second cover quench oil system quenching oil column tower reactor is sent in the pyrolyzer and is mixed with splitting gas, the gas-oil mixture that obtains is sent into the visbreaking tower of first set quench oil system, the visbreaking top gaseous phase is admitted to first set quenching system quenching oil tower reactor, visbreaking tower reactor liquid phase is divided into three strands, one is got back to the visbreaking tower reactor and forms self circulation, another thigh is delivered to first set quenching oil column tower reactor, remaining one delivered to the tank field as product, and the quenching oil of first set quenching oil column tower reactor is sent the second cover quenching oil column tower reactor back to and kept the second cover quenching oil column tower reactor liquid level.
2. the technique of a kind of two cover quench oil system Reduce viscosities according to claim 1 is characterized in that described pyrolyzer is ethane cracking furnace or ethane and Deposition During Propane Pyrolysis stove.
3. the techniques of a kind of two cover quench oil system Reduce viscosities according to claim 1, it is characterized in that, described quenching oil is the single loop circulation between two quenching oil columns and visbreaking tower, first set quench oil system part quenching oil is sent to the second cover quench oil system, and the second cover quench oil system part quenching oil returns again the first set quench oil system through the visbreaking tower.
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| CN103305257B (en) * | 2012-03-16 | 2015-04-15 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
| CN103305258B (en) * | 2012-03-16 | 2015-06-17 | 中国石油化工股份有限公司 | Method for reducing viscosity of quenching oil of ethylene unit |
| CN104449826B (en) * | 2013-09-13 | 2016-05-25 | 中国石油化工股份有限公司 | A kind of method that reduces ethylene unit quench oil viscosity |
| CN111876194A (en) * | 2020-08-05 | 2020-11-03 | 山东京博石油化工有限公司 | Naphtha cracking device and method for producing steam |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001139961A (en) * | 1999-11-17 | 2001-05-22 | Toyo Eng Corp | Removal of heavy fraction of ethylene plant decomposition gas |
| CN101074184A (en) * | 2006-05-18 | 2007-11-21 | 中国石油天然气股份有限公司 | Viscosity reducing method for quenching oil of ethylene unit |
| CN101323553A (en) * | 2007-06-13 | 2008-12-17 | 中国石油天然气股份有限公司 | Method for increasing temperature of ethylene unit quenching oil tower bottom |
-
2010
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001139961A (en) * | 1999-11-17 | 2001-05-22 | Toyo Eng Corp | Removal of heavy fraction of ethylene plant decomposition gas |
| CN101074184A (en) * | 2006-05-18 | 2007-11-21 | 中国石油天然气股份有限公司 | Viscosity reducing method for quenching oil of ethylene unit |
| CN101323553A (en) * | 2007-06-13 | 2008-12-17 | 中国石油天然气股份有限公司 | Method for increasing temperature of ethylene unit quenching oil tower bottom |
Non-Patent Citations (2)
| Title |
|---|
| 减粘塔技术在乙烯急冷系统改造中的应用;许岩峰;《乙烯工业》;20091231;第21卷(第2期);12-19 * |
| 许岩峰.减粘塔技术在乙烯急冷系统改造中的应用.《乙烯工业》.2009,第21卷(第2期),12-19. |
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