CN101962570A - Method for producing high-octane gasoline by hydrocracking distillate oil of low-grade petroleum - Google Patents
Method for producing high-octane gasoline by hydrocracking distillate oil of low-grade petroleum Download PDFInfo
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- CN101962570A CN101962570A CN2010105221337A CN201010522133A CN101962570A CN 101962570 A CN101962570 A CN 101962570A CN 2010105221337 A CN2010105221337 A CN 2010105221337A CN 201010522133 A CN201010522133 A CN 201010522133A CN 101962570 A CN101962570 A CN 101962570A
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Abstract
The invention relates to a method for producing high-octane gasoline by hydrocracking distillate oil of low-grade petroleum, which belongs to the technical field of petroleum refining. The method is as follows: carrying out hydrocracking ring opening and cracking reaction on distillate raw materials including straight-run distillate oil produced by atmospheric and vacuum distillation one-time processing production of the petroleum, light cycle oil produced by a catalytic cracking device, the distillate oil produced by a delayed coking device, light deasphalted oil which removes asphalt in solvent and the like of low-grade petroleum in the presence of hydrogen partial pressure and a bifunctional catalyst, and then producing blended components of the high-octane gasoline which is rich in mononuclear aromatics and the research octane number RON of 80-96, wherein the distillation range of the distillate raw materials is 160-450 DEG C. The invention provides a brand new way for upgrading the quality of the gasoline and diesel to the standard which is equivalent to European Union IV (the sulfur content in the finished product gasoline is below 50ppm, and the sulfur content in the diesel is below 50ppm) and European Union V (the sulfur content in the finished product gasoline is below 10ppm, and the sulfur content in the diesel is below 30ppm).
Description
Technical field
The present invention relates to the method that stop bracket gasoline is produced in the fraction oil of petroleum hydrocracking inferior of a kind of usefulness, belong to the petroleum refining technology field.
Background technology
At present, known hydrocracking refining process, be a kind of be raw material with the heavier petroleum fraction, in the presence of hydrogen dividing potential drop and dual-function catalyst, through hydrocracking reaction, be the refining process of purpose with production high-quality light oil products (as petroleum naphtha, rocket engine fuel, low freezing point diesel fuel etc.).Hydrocracking is the important process means that refinery is produced clean fuel.
One of purpose product that known hydrocracking refining process produces is a petroleum naphtha.The hydrocracking petroleum naphtha is low excessively because of octane value (RON=60～75), generally can not be as the mediation component of commercial gasoline, but carry out deep processing as the raw material of cracking of ethylene or reformer.
Another purpose product that known hydrocracking refining process produces is a solar oil.When the raw material of hydrocracking was fraction oil of petroleum inferior, the cetane value of the solar oil of its production (cetane value=30～40) was on the low side, is difficult to the mediation component as solar oil, reconciles into the commodity solar oil and dispatches from the factory.
A difficult problem that when the frivolous wet goods of the distillate of handling straight run oil that fraction oil of petroleum one atmospheric and vacuum distillation of petroleum time processing inferior produces, light cycle oil that catalytic cracking unit is produced, delayed coker produces and solvent deasphalting, is faced, the one, because the not fully cracking of dicyclo or tricyclic compound, cause solar oil cut cetane value on the low side, be difficult to mediation component as the commodity solar oil; The 2nd, because the fully cracking of dicyclo or tricyclic compound, cause in the naphtha fraction aromaticity content on the low side, make octane value low excessively, be difficult to mediation component as commercial gasoline.
Summary of the invention
The purpose of this invention is to provide the method that stop bracket gasoline is produced in the fraction oil of petroleum hydrocracking inferior of a kind of usefulness, overcome the shortcoming of prior art, dicyclo or tricyclic compound with the band side chain in the petroleum fractions raw material inferior, in the presence of hydrogen dividing potential drop and dual-function catalyst, through hydrocracking open loop, cracking reaction, be rich in the stop bracket gasoline mediation component of mononuclear aromatics with production.
The method that stop bracket gasoline is produced in the usefulness that the present invention proposes fraction oil of petroleum hydrocracking inferior may further comprise the steps:
(1) the oil inferior distillate oil is heated to 300 ℃～420 ℃, mixes with hydrogen, the blended hydrogen to oil volume ratio is: 100: 1～1500: 1, obtain incoming mixture;
(2) make the bed of above-mentioned incoming mixture by being made up of first catalyzer, volume space velocity is 0.5hr
-1～4hr
-1, reaction pressure is 5MPa～20MPa, removes sulphur, nitrogen impurity in the incoming mixture, and makes ring of two in the incoming mixture or tricyclic compound fractional saturation, obtains treated oil;
(3) make the bed of above-mentioned refining oil-hydrogen mixture by being made up of second catalyzer, volume space velocity is 0.5hr
-1～2.0hr
-1, temperature of reaction is 350 ℃～450 ℃, and reaction pressure is 5MPa～20MPa, and hydrogen to oil volume ratio is: 100: 1～1500: 1, make two ring or tricyclic compound crackings of band side chain in the treated oil, obtain being rich in the reaction product of mononuclear aromatics;
(4) above-mentioned reaction product is cooled to 30 ℃～50 ℃, separates obtaining the hydrogen and first liquid phase;
(5) make above-mentioned first liquid phase be decompressed to 0.1MPa～0.5MPa, isolate the gas and second liquid phase;
(6) to the heating of above-mentioned second liquid phase, Heating temperature is 180 ℃～370 ℃, carries out fractionation, obtains stop bracket gasoline at the side exit of separation column.
In the aforesaid method, described first catalyzer is a Hydrobon catalyst.
In the aforesaid method, described second catalyzer is a hydrocracking catalyst.
The method that stop bracket gasoline is produced in the usefulness that the present invention proposes fraction oil of petroleum hydrocracking inferior has the following advantages:
1, the inventive method has overcome the shortcoming of prior art, hydrocracking reaction process by dicyclo or tricyclic compound in the change oil inferior distillate oil, make it be converted into the mononuclear aromatics of band side chain to greatest extent, thereby solved the on the low side and diesel product cetane value difficult problem on the low side of naphtha product octane value that known hydrocracking process is faced when handling fraction oil of petroleum inferior, produced high value-added product.
2, the inventive method is brought up to RON=80～96 with the octane value of hydrocracking petroleum naphtha by RON=60～75, makes it become the ideal mediation component that fine does not have alkene, super low sulfur (5 μ g/g～10 μ g/g), stop bracket gasoline; Simultaneously with the cetane value of hydrocracking solar oil, bring up to 45～50 by 30～40, make its ideal that becomes fine low-sulfur, low density, high hexadecane value, high oxidation stability solar oil be in harmonious proportion component.
3, the inventive method is that gasoline, diesel quality are upgraded to and are equivalent to the IV of European Union (below the gasoline product sulphur content 50ppm, diesel oil sulphur content 50ppm is following) and the V of European Union (below the gasoline product sulphur content 10ppm, below the diesel oil sulphur content 30ppm) standard a brand-new approach is provided.
Embodiment
The method that stop bracket gasoline is produced in the usefulness that the present invention proposes fraction oil of petroleum hydrocracking inferior may further comprise the steps:
(1) the oil inferior distillate oil is heated to 300 ℃～420 ℃, mixes with hydrogen, the blended hydrogen to oil volume ratio is: 100: 1～1500: 1, obtain incoming mixture;
(2) make the bed of above-mentioned incoming mixture by being made up of first catalyzer, volume space velocity is 0.5hr
-1～4hr
-1, reaction pressure is 5MPa～20MPa, removes sulphur, nitrogen impurity in the incoming mixture, and makes ring of two in the incoming mixture or tricyclic compound fractional saturation, obtains treated oil;
(3) make the bed of above-mentioned refining oil-hydrogen mixture by being made up of second catalyzer, volume space velocity is 0.5hr
-1～2.0hr
-1, temperature of reaction is 350 ℃～450 ℃, and reaction pressure is 5MPa～20MPa, and hydrogen to oil volume ratio is: 100: 1～1500: 1, make two ring or tricyclic compound crackings of band side chain in the treated oil, obtain being rich in the reaction product of mononuclear aromatics;
(4) above-mentioned reaction product is cooled to 30 ℃～50 ℃, separates obtaining the hydrogen and first liquid phase;
(5) make above-mentioned first liquid phase be decompressed to 0.1MPa～0.5MPa, isolate the gas and second liquid phase;
(6) to the heating of above-mentioned second liquid phase, Heating temperature is 180 ℃～370 ℃, carries out fractionation, obtains stop bracket gasoline at the side exit of separation column.
In the aforesaid method, described first catalyzer is a Hydrobon catalyst.
In the aforesaid method, described second catalyzer is a hydrocracking catalyst.
The first used catalyzer of the embodiment of the invention is produced by Fushun Petrochemical Company company of CNPC, model is 3996, second catalyzer is the non-noble metal supported catalyzer that is used for distillate hydrocracking, and embodiment has shown the technology assessment result of this catalyst performance.
Second catalyzer that uses in the various embodiments of the present invention, its preparation method is as follows:
(1) takes by weighing 50 gram NaY molecular sieves under 60 ℃～95 ℃, with mass percent concentration is that the ammonium salt of 0.50wt% exchanges, be swap time: 6 hours, filter, washing, 100 ℃ of dryings 6 hours, repeat above step 3 time, 800 ℃ of following hydrothermal treatment consists 2 hours, after washing, under air atmosphere,, make big silica alumina ratio molecular sieve Y in 100 ℃ of dryings 18 hours.
(2) take by weighing 33.800 gram tetraethyl ammonium hydroxides (template, Hangzhou Yan Shan chemical industry company limited Industrial products, concentration 35%), add 20.200 gram H
2The O dilution adds 3.280 gram sodium metaaluminate (NaAlO again
2, Tianjin, Tianjin fine chemistry industry institute of section, chemically pure reagent) and 1.667 gram sodium hydroxide (Beijing chemical reagent factories, chemically pure reagent, purity＞96%), be dissolved to the transparent working fluid of making at 80 ℃, in working fluid, add 61.224 gram silochrom (Qingdao Marine Chemical Co., Ltd., SiO
2Content 98%), be stirred under 60 ℃ evenly, template state of being evenly distributed in system makes clear liquor, and the composition of each material in this clear liquor is counted by mole: SiO
2: Al
2O
3: Na
2O: template: water=100: 2.0: 4: 20: 300.The clear liquor that stirs is transferred in the autoclave of 200ml, adopt to be divided a temperature section crystallization,, be warmed up to 175 ℃ of crystallization 15 hours again 135 ℃ of crystallization 20 hours; With the product that obtains filter, washing, under air atmosphere in 100 ℃ of dryings 16 hours, took off amine 18 hours 535 ℃ of following roastings, promptly get big silica-alumina ratio beta 1 zeolite product of the present invention.
(3) take by weighing above-mentioned 30.0 gram Y molecular sieves that make and 70.0 gram β, 1 molecular sieve, 50.0 amorphous aluminum silicides that restrain, 20 gram macroporous aluminium oxides and 5.5 gram sesbania powder mixed grind 30min, the mass percent of each component is in this mixture: big silica alumina ratio molecular sieve β+Y is: 56.98wt%, wherein big silica alumina ratio molecular sieve Y: big silica alumina ratio molecular sieve β=1: 2.33, amorphous silicon aluminium is: 28.5wt%, the porous refractory oxide is: 11.4wt%, and extrusion aid sesbania powder is: 3.1wt%; Add 210.0 grams then and be prepared into the tackiness agent mixing with little porous aluminum oxide and dilute nitric acid solution, rare concentration of nitric acid=1.5% in the tackiness agent, concentration=the 5wt% of little porous aluminum oxide, continue to roll to squeezing cream and stick with paste, be extruded into the cylinder shape stripe shape, extrude bar 120 ℃ of dryings 6 hours, 525 ℃ of roastings of dried strip temperature programming 8 hours make support of the catalyst 1.
(4) get Ni (NO3) 2.6H2O, (NH4) 2W4O13.4H2O, add water preparation steeping fluid, WO in the steeping fluid
3Volumetric concentration=7.38g/100ml, volumetric concentration=1.56g/100ml of NiO, steeping fluid with gained floods the support of the catalyst of making according to above-described method 1, liquid-solid ratio=2.0 of dipping, dipping temperature is 25 ℃, and dipping time is 24 hours, and the carrier 1 that above-mentioned dipping is good is following dry 8 hours at 120 ℃, the carrier 1 that above-mentioned drying is good makes catalyzer HC1 525 ℃ of following roastings 12 hours.Catalyzer HC1 metal and molecular sieve weight are formed: WO
3Content=26.0wt%, NiO content=5.5wt%, big silica alumina ratio molecular sieve Y=11.4wt%, β 1=26.6wt%, specific surface area 276.5m
2/ g, pore volume 0.37ml/g.
Below introduce the embodiment of the inventive method.
Embodiment 1
(1) oil inferior distillate oil raw material 1 is heated to 320 ℃, under reaction pressure 10.0MPa, mixes with hydrogen, the blended hydrogen to oil volume ratio is: 1000: 1, obtain incoming mixture;
(2) make the bed of above-mentioned incoming mixture by being made up of first catalyzer, volume space velocity is 0.5hr
-1, remove sulphur, nitrogen impurity in the incoming mixture, and make ring of two in the incoming mixture or tricyclic compound fractional saturation, obtain treated oil;
(3) make the bed of above-mentioned refining oil-hydrogen mixture by being made up of second catalyzer, volume space velocity is 0.6hr
-1, temperature of reaction is 400 ℃, reaction pressure is 10MPa, makes two ring or tricyclic compound crackings of band side chain in the treated oil, obtains being rich in the reaction product of mononuclear aromatics;
(4) above-mentioned reaction product is cooled to 40 ℃, separates obtaining the hydrogen and first liquid phase;
(5) make above-mentioned first liquid phase be decompressed to 0.35MPa, isolate the gas and second liquid phase;
(6) to the heating of above-mentioned second liquid phase, Heating temperature is 370 ℃, carries out fractionation, obtains stop bracket gasoline at the side exit of separation column.
Separation column is partitioned into lighter hydrocarbons, stop bracket gasoline, solar oil product with charging and goes out device and unconverted tail oil; The cracking that all circulates of unconverted tail oil.The raw material of present embodiment is formed and evaluation result sees Table 1 and table 2 respectively.
Embodiment 2
(1) oil inferior distillate oil raw material 2 is heated to 300 ℃, under reaction pressure 16.0MPa, mixes with hydrogen, the blended hydrogen to oil volume ratio is: 800: 1, obtain incoming mixture;
(2) make the bed of above-mentioned incoming mixture by being made up of first catalyzer, volume space velocity is 1.0hr
-1, remove sulphur, nitrogen impurity in the incoming mixture, and make ring of two in the incoming mixture or tricyclic compound fractional saturation, obtain treated oil;
(3) make the bed of above-mentioned refining oil-hydrogen mixture by being made up of second catalyzer, volume space velocity is 1.0hr
-1, temperature of reaction is 390 ℃, reaction pressure is 16MPa, makes two ring or tricyclic compound crackings of band side chain in the treated oil, obtains being rich in the reaction product of mononuclear aromatics;
(4) above-mentioned reaction product is cooled to 40 ℃, separates obtaining the hydrogen and first liquid phase;
(5) make above-mentioned first liquid phase be decompressed to 0.35MPa, isolate the gas and second liquid phase;
(6) to the heating of above-mentioned second liquid phase, Heating temperature is 370 ℃, carries out fractionation, obtains stop bracket gasoline at the side exit of separation column.
Separation column is partitioned into lighter hydrocarbons, stop bracket gasoline, solar oil product with charging and goes out device and unconverted tail oil; The cracking that all circulates of unconverted tail oil.The raw material of present embodiment is formed and evaluation result sees Table 1 and table 2 respectively.
Embodiment 3
(1) oil inferior distillate oil raw material 3 is heated to 300 ℃, under reaction pressure 12MPa, mixes with hydrogen, the blended hydrogen to oil volume ratio is: 1500: 1, obtain incoming mixture;
(2) make the bed of above-mentioned incoming mixture by being made up of first catalyzer, volume space velocity is 0.8hr
-1, remove sulphur, nitrogen impurity in the incoming mixture, and make ring of two in the incoming mixture or tricyclic compound fractional saturation, obtain treated oil;
(3) make the bed of above-mentioned refining oil-hydrogen mixture by being made up of second catalyzer, volume space velocity is 1.8hr
-1, temperature of reaction is 410 ℃, reaction pressure is 12MPa, makes two ring or tricyclic compound crackings of band side chain in the treated oil, obtains being rich in the reaction product of mononuclear aromatics;
(4) above-mentioned reaction product is cooled to 40 ℃, separates obtaining the hydrogen and first liquid phase;
(5) make above-mentioned first liquid phase be decompressed to 0.35MPa, isolate the gas and second liquid phase;
(6) to the heating of above-mentioned second liquid phase, Heating temperature is 370 ℃, carries out fractionation, obtains stop bracket gasoline at the side exit of separation column.
Separation column is partitioned into lighter hydrocarbons, stop bracket gasoline, solar oil product with charging and goes out device and unconverted tail oil; The cracking that all circulates of unconverted tail oil.The raw material of present embodiment is formed and evaluation result sees Table 1 and table 2 respectively.
Comparative Examples 1,2
Second catalyzer that Comparative Examples 1,2 adopts is different with embodiment 1.
Comparative Examples 1 used second catalyzer is 3976 hydrocracking catalysts that Fushun petrochemical Corp., CNPC produces.
Comparative Examples 2 used second catalyzer are 3963 hydrocracking catalysts that Fushun petrochemical Corp., CNPC produces.
The evaluation raw material that Comparative Examples 1,2 adopts, evaluation processing condition and embodiment 1 are identical, and its evaluation result is also listed in table 2.
Table 1 raw material oil properties
| The raw material numbering | Raw material 1 | Raw material 2 | Raw material 3 |
| Embodiment | 1, Comparative Examples 1,2 | 2 | 3 |
| Boiling range, ℃ | |||
| HK/5％ | 175/204 | 165/198 | 165/196 |
| 10％/30％ | 214/238 | 213/241 | 209/235 |
| 50％/70％ | 253/281 | 255/291 | 245/275 |
| 90％/KK | 335/353 | 338/365 | 336/358 |
| Density (20 ℃), g/cm 3 | 0.9076 | 0.9010 | 0.9240 |
| Cetane value | 26.0 | 28.5 | 20.0 |
| Condensation point, ℃ | -17 | -8 | -15 |
| Total sulfur, μ g/g | 57 | 2500 | 2000 |
| Total nitrogen, μ g/g | 81 | 856 | 267 |
| Carbon residue, % | 0.038 | 0.042 | 0.025 |
| Group composition, wt% | |||
| Alkene | 3.5 | 5.8 | 0 |
| Alkane | 29.1 | 30.2 | 24.6 |
| Aromatic hydrocarbons | 67.4 | 64.0 | 75.4 |
Table 2 evaluation result
| Embodiment | 1 | 2 | 3 | Comparative Examples 1 | Comparative Examples 2 |
| The Hydrobon catalyst trade mark | 3996 | 3996 | 3996 | 3996 | 3996 |
| The hydrocracking catalyst numbering | HC1 | HC1 | HC1 | 3976 | 3963 |
| Average reaction temperature, ℃ | 410 | 410 | 415 | 415 | 417 |
| The C5+ liquid yield, wt% | 99.0 | 99.2 | 98.6 | 96.5 | 95.5 |
| ＞300 ℃ of transformation efficiencys, % | 70 | 70 | 70 | 70 | 70 |
| Product distributes and oil property | |||||
| HK～180 ℃ gasoline | |||||
| Yield, % | 55.0 | 56.1 | 54.7 | 51.5 | 51.6 |
| RON | 92.5 | 91.7 | 93.2 | 65.5 | 68.0 |
| 180～350 ℃ of diesel oil | |||||
| Yield, % | 44.0 | 43.1 | 43.9 | 45.0 | 43.9 |
| Density (20 ℃), g/cm 3 | 0.8380 | 0.8410 | 0.8406 | 0.8430 | 0.8460 |
| Cetane value | 45.0 | 48.5 | 43.5 | 37.5 | 39.0 |
| Condensation point, ℃ | -28 | -19 | -11 | -27 | -25 |
Claims (3)
1. method of producing stop bracket gasoline with fraction oil of petroleum hydrocracking inferior is characterized in that this method may further comprise the steps:
(1) the oil inferior distillate oil is heated to 320 ℃～420 ℃, mixes with hydrogen, the blended hydrogen to oil volume ratio is: 100: 1～1500: 1, obtain incoming mixture;
(2) make the bed of above-mentioned incoming mixture by being made up of first catalyzer, volume space velocity is 0.5hr
-1～4hr
-1, reaction pressure is 5MPa～20MPa, removes sulphur, nitrogen impurity in the incoming mixture, and makes ring of two in the incoming mixture or tricyclic compound fractional saturation, obtains treated oil;
(3) make the bed of above-mentioned refining oil-hydrogen mixture by being made up of second catalyzer, volume space velocity is 0.5hr
-1～2.0hr
-1, temperature of reaction is 350 ℃～450 ℃, and reaction pressure is 5MPa～20MPa, and hydrogen to oil volume ratio is: 100: (1～1500): 1, make two ring or tricyclic compound crackings of band side chain in the treated oil, obtain being rich in the reaction product of mononuclear aromatics;
(4) above-mentioned reaction product is cooled to 30 ℃～50 ℃, separates obtaining the hydrogen and first liquid phase;
(5) make above-mentioned first liquid phase be decompressed to 0.1MPa～0.5MPa, isolate the gas and second liquid phase;
(6) to the heating of above-mentioned second liquid phase, Heating temperature is 180 ℃～210 ℃, carries out fractionation, obtains stop bracket gasoline at the side exit of separation column.
2. the method for claim 1 is characterized in that wherein said first catalyzer is a Hydrobon catalyst.
3. the method for claim 1 is characterized in that wherein said second catalyzer is a hydrocracking catalyst.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102732298A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Liquid phase hydrogenation method |
| CN104109557A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Catalytic conversion method of inferior distillate oil or heavyweight oil |
| CN104611062A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | High octane number gasoline production method |
| CN106047404A (en) * | 2016-07-08 | 2016-10-26 | 中海油天津化工研究设计院有限公司 | Combined technique for improving yield of high-octane gasoline by using inferior catalytic cracking diesel |
| CN110551526A (en) * | 2018-05-30 | 2019-12-10 | 中国石油化工股份有限公司 | Processing method of catalytic cracking light cycle oil |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4919789A (en) * | 1985-06-03 | 1990-04-24 | Mobil Oil Corp. | Production of high octane gasoline |
| CN1952076A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Paraffin-hydrogenating refining process |
| CN101724454A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Hydrocracking method for producing high-octane petrol |
-
2010
- 2010-10-22 CN CN201010522133.7A patent/CN101962570B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4919789A (en) * | 1985-06-03 | 1990-04-24 | Mobil Oil Corp. | Production of high octane gasoline |
| CN1952076A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Paraffin-hydrogenating refining process |
| CN101724454A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Hydrocracking method for producing high-octane petrol |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102732298A (en) * | 2011-04-12 | 2012-10-17 | 中国石油化工股份有限公司 | Liquid phase hydrogenation method |
| CN104109557A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Catalytic conversion method of inferior distillate oil or heavyweight oil |
| CN104109557B (en) * | 2013-04-16 | 2016-03-02 | 中国石油化工股份有限公司 | The catalysis conversion method of a kind of inferior distillate oil or heavy oil product |
| CN104611062A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | High octane number gasoline production method |
| CN104611062B (en) * | 2013-11-05 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of high-knock rating gasoline production method |
| CN106047404A (en) * | 2016-07-08 | 2016-10-26 | 中海油天津化工研究设计院有限公司 | Combined technique for improving yield of high-octane gasoline by using inferior catalytic cracking diesel |
| CN110551526A (en) * | 2018-05-30 | 2019-12-10 | 中国石油化工股份有限公司 | Processing method of catalytic cracking light cycle oil |
| CN110551526B (en) * | 2018-05-30 | 2021-08-06 | 中国石油化工股份有限公司 | Processing method of catalytic cracking light cycle oil |
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| CN101962570B (en) | 2014-01-15 |
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