CN103160317B - Production method of propylene and gasoline with high-octane rating - Google Patents
Production method of propylene and gasoline with high-octane rating Download PDFInfo
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- CN103160317B CN103160317B CN201110419546.7A CN201110419546A CN103160317B CN 103160317 B CN103160317 B CN 103160317B CN 201110419546 A CN201110419546 A CN 201110419546A CN 103160317 B CN103160317 B CN 103160317B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
A production method of propylene and gasoline with high-octane rating. The method is as below: introducing catalytic cracking heavy oil from a catalytic cracking unit into a hydrogenation unit; contacting the catalytic cracking heavy oil with a hydrogenation catalyst under hydrogenation reaction conditions for reaction; controlling hydrogenation severity of the hydrogenation unit, so that after hydrogenation of the catalytic cracking heavy oil, 10-80 wt% of polycyclic aromatic hydrocarbons is subjected to hydrogen saturation into cycloalkanes; and sending the hydrogenated oil into the catalytic cracking unit for a cracking reaction to produce propylene and gasoline with high-octane rating. The invention can greatly improve the cracking performance of catalytic cracking heavy oil, thus improving the conversion and the yield of light oil of the catalytic cracking unit, and realizing efficient utilization of oil resources.
Description
Technical field
The present invention relates to a kind of working method of hydrocarbon ils, more particularly, be a kind of by hydrogenation unit and catalytic cracking unit associating, processing catalytic cracking heavy oil produces the method for propylene and stop bracket gasoline.
Background technology
International oil price continues soaring in recent years, and the petroleum products demand of China's Economic development to high value constantly increases, and existing market continues the aggravation of contradictions of heaviness and in poor quality to the continuous lighting of petroleum products, high quality and the requirement cleaned and oil supply.Therefore promote the limited heavy oil resources degree of depth and transform efficiently, increasing light-end products is significant challenge that China's oil refining industry faces.Meanwhile, along with increasing rapidly of the derivative demands such as polypropylene, market is also all increasing year by year to the demand of propylene.
Catalytic cracking technology is that inferior heavy oil is converted into one of the most effective technology of lightweight oil, is also the Main Means producing propylene simultaneously.In the U.S., almost 50% of propylene market demand all derive from catalytic cracking unit.Existing catalytic cracking unit is in order to increase transformation efficiency and the yield of light oil of catalytic cracking, usually heavy oil (heavy cycle oil) repeats itself in catalytic cracking unit catalytic unit produced, but because the hydrogen richness of catalytic cracking heavy oil is low, polycyclic aromatic hydrocarbon content is high, and its cracking effect is unsatisfactory.A big chunk of catalytic cracking heavy oil is converted into coke, adds For Fcc Regenerator load, reduces treatment capacity and the petrol and diesel oil product yield of catalytic cracking unit.
CN101531923A proposes a kind of method of being produced propylene and light Fuel by inferior feedstock oil.Inferior feedstock oil is through hydrotreatment, and the hydrogenated residue obtained obtains propylene, gasoline, catalytic cracking heavy oil and other products through catalytic cracking, and wherein catalytic cracking heavy oil enters hydrotreater; Catalytic cracking heavy oil after hydrogenation is circulated to catalytic cracking unit and is obtained by reacting object product propylene and gasoline further.
Summary of the invention
The object of the invention is on the basis of existing technology, a kind of method providing hydrotreatment and catalytic cracking to combine, produces propylene and stop bracket gasoline by catalytic cracking heavy oil.
Method provided by the invention is:
Catalytic cracking heavy oil from catalytic cracking unit enters hydrogenation unit, contact with hydrogenation catalyst under hydrogenation conditions and react, the hydrogenated oil of gained enters catalytic cracking unit and carries out cracking reaction further, obtain object product propylene and gasoline, by controlling the hydrogenation severity of hydrogenation unit, make catalytic cracking heavy oil after hydrotreatment, 10 % by weight ~ 80 % by weight hydrotreated lube base oil of contained polycyclic aromatic hydrocarbons are naphthenic hydrocarbon.Catalytic cracking heavy oil and hydrogen mix to contact with hydrogenation catalyst and react.
Described catalytic cracking heavy oil refers to that catalytic cracking feeds is converted into unconverted part outside gas, light-end products (gasoline and diesel oil) and coke in catalytic cracking unit, and the boiling range of described catalytic cracking heavy oil is 260 DEG C ~ 550 DEG C.Catalytic cracking heavy oil aromaticity content is high, and mainly polycyclic aromatic hydrocarbons, wherein polycyclic aromatic hydrocarbon content is greater than 30 % by weight, is preferably greater than 35 % by weight.
In the method, catalytic cracking heavy oil is after hydrotreatment, and wherein part polycyclic aromatic hydrocarbons hydrotreated lube base oil generates naphthenic hydrocarbon, and naphthenic hydrocarbon can produce propylene and stop bracket gasoline through further catalytic cracking.Therefore in hydrogenated oil, the content of naphthenic hydrocarbon is higher, is more conducive to producing more propylene.In addition, catalytic cracking heavy oil can also reduce sulphur, nitrogen content after hydrotreatment.The reduction of sulphur content can reduce the sulphur content of catalytically cracked gasoline, reduces the discharge of revivifier SOx.Because nitrogen compound can make the active centre of acidic catalyst cracking catalyst poisoning, active reduction, transformation efficiency declines, and therefore the reduction of nitrogen content can improve transformation efficiency and the product yield of catalytic cracking heavy oil.
The present invention is using the change of hydrogen richness in catalytic cracking heavy oil and hydrogenated oil as the parameter characterizing hydrogenation severity.The present inventor is found by research, and in catalytic cracking heavy oil hydrogenated oil, the content of mononuclear aromatics is associated with hydrogenation severity.Before and after catalytic cracking heavy oil hydrogenation, the change (Δ H) of hydrogen richness is as the parameter characterizing hydrogenation severity.As shown in drawings, under lower hydrogenation severity, with the raising of hydrogenation severity, in hydrogenated oil, the content of naphthenic hydrocarbon increases, and this is because polycyclic aromatic hydrocarbons hydrotreated lube base oil generates naphthenic hydrocarbon.When hydrogenation severity is increased to a degree, the naphthene content in hydrogenated oil no longer increases, and this is mainly owing to there being the hydrocracking of part naphthenic hydrocarbon to generate paraffinic hydrocarbons.If improve hydrogenation severity further again, the hydrogen of consumption will be mainly used in hydrocracking reaction, instead of the hydrotreated lube base oil reaction of polycyclic aromatic hydrocarbons.Hydrogen is one of main cost of hydroprocessing processes.Therefore hydrogenation severity to be controlled in the hydroprocessing processes of catalytic cracking heavy oil in one reasonably interval (in figure dash area), so just the highest hydrogenated oil of naphthene content can be obtained under the condition consuming hydrogen less as far as possible.The control of hydrogenation severity can be realized by adjusting process condition.Processing condition mainly comprise, hydrogen dividing potential drop, temperature of reaction, volume space velocity and hydrogen-oil ratio.
The reaction conditions of described hydrogenation unit is: hydrogen dividing potential drop 5.0MPa ~ 19.0MPa, preferred 6.0MPa ~ 18.0MPa, temperature of reaction 330 DEG C ~ 410 DEG C, preferably 340 DEG C ~ 400 DEG C, hydrogen to oil volume ratio 100Nm
3/ m
3~ 1800Nm
3/ m
3, preferred 200Nm
3/ m
3~ 1200Nm
3/ m
3, volume space velocity 0.2h
-1~ 1.8h
-1, preferred 0.3h
-1~ 1.5h
-1.
Described hydrogenation catalyst comprise according to incoming flow to; the hydrogenation protecting agent of loading successively, the agent of hydrogenation diasphaltene and hydrofining agent; with hydrogenation unit integer catalyzer volume for benchmark; the admission space percentage ratio of described hydrogenation protecting agent, the agent of hydrogenation diasphaltene and hydrofining agent is respectively 2% ~ 30%, 5% ~ 50% and 5% ~ 93%.
Described hydrogenation protecting agent is Raschig ring shape; containing molybdenum on this alumina supporter of a kind of alumina supporter and load and/or tungsten; and nickel and/or cobalt; with the gross weight of hydrogenation protecting agent for benchmark; and with oxide basis; the content of molybdenum and/or tungsten is 1 ~ 10 % by weight, and the content of nickel and/or cobalt is 0.5 ~ 3 % by weight.Described aluminum oxide is gama-alumina, and the pore volume of described hydrogenation protecting agent is not less than 0.50ml/g, is preferably not less than 0.60ml/g.This hydrogenation protecting agent has low coke content, low pore volume rate of descent, good activity stability and high intensity.The present invention loads the larger hydrogenation protecting agent of voidage on the top of reactor; the tiny catalytic cracking catalyst powder carried secretly in raw material can be removed further; simultaneously can the foulant of easy green coke in effective elimination raw material; reach the object of protection hydrogenation Primary Catalysts, ensure hydrotreater long-time running.
Described hydrogenation diasphaltene agent is butterfly-type, containing a kind of carrier and load molybdenum on this carrier and/or tungsten, and nickel and/or cobalt, with the gross weight of hydrogenation diasphaltene agent for benchmark, and with oxide basis, the content of molybdenum and/or tungsten is 0.5 ~ 18 % by weight, the content of nickel and/or cobalt is 0.3 ~ 10 % by weight, carrier is aluminum oxide and optional silicon oxide, and described hydrogenation diasphaltene agent pore volume is not less than 0.60ml/g, is preferably not less than 0.70ml/g.The asphalt content of conventional wax oil hydrogenation refining plant design charging generally should be less than 500 μ g/g, and the asphalt content in catalytic cracking heavy oil is at 3000 μ about g/g, far above the requirement of conventional Wax Oil Hydrogenation Unit design charging.And, bituminous matter is component the heaviest in catalytic cracking heavy oil, and be green coke precursor main in catalytic cracking heavy oil, molecular dimension often reaches more than tens nanometers, easily cause catalyzer coking and deactivation, affect the work-ing life of catalyst activity stability and shortening catalyzer.Therefore to load the hydrogenation diasphaltene agent of large pore volume after hydrogenation protecting agent, make the bituminous matter in raw material obtain partial removal, to reach the object of protection rear portion hydrofining agent.
Described hydrofining agent is butterfly-type, containing a kind of carrier and load molybdenum on this carrier and/or tungsten, and nickel and/or cobalt, with the gross weight of hydrofining agent for benchmark, and with oxide basis, the content of molybdenum and/or tungsten is 10 ~ 40 % by weight, the content of nickel and/or cobalt is 0.3 ~ 7 % by weight, carrier is aluminum oxide and optional silicon oxide, and hydrofining agent pore volume is not less than 0.25ml/g, is preferably not less than 0.30ml/g.After hydrogenation diasphaltene catalyzer, load Hydrobon catalyst, this catalyzer has much higher Polycyclic aromatic hydrocarbons saturated activity, has high desulfurization and denitrification activity simultaneously.
In the present invention, catalytic cracking unit can be a set of or a set of above catalytic cracking unit, and every covering device at least should comprise a reactor, a revivifier and a separation column.The catalytic cracking catalyst that catalytic cracking unit uses is REY, REHY, ZSM-5 molecular sieve catalyzer or mixture, processing condition are: the weight ratio (hereinafter referred to as agent-oil ratio) 3 ~ 10 of temperature of reaction 470 DEG C ~ 570 DEG C, 0.5 second ~ 5 seconds reaction times, catalyzer and stock oil, regeneration temperature 650 DEG C ~ 800 DEG C.
Advantage of the present invention is:
(1), the present invention greatly can improve the cracking performance of catalytic cracking heavy oil, thus improve catalytic cracking unit transformation efficiency and yield of light oil, realizes the efficiency utilization of petroleum resources.
(2), the present invention controls hydrogenation severity in rational interval by adjustment catalytic cracking heavy oil hydrogenation process conditions, the hydrogenated oil being rich in naphthenic hydrocarbon can be obtained, and obtain more propylene and high-octane gasoline products by follow-up catalytic cracking process.
Accompanying drawing explanation
Accompanying drawing is the graph of a relation of naphthene content in the hydrogenation severity of hydrogenation unit and hydrogenated oil.
Embodiment
The following examples will be further described the present invention, but therefore not limit the present invention.
The catalytic cracking heavy oil character adopted in embodiment is in table 1.The filling ratio of the hydrogenation protecting agent that catalytic cracking heavy oil hydropyrolysis experiment adopts, the agent of hydrogenation diasphaltene and hydrofining agent is 5: 15: 80; wherein the trade names of hydrogenation protecting agent are respectively RG-10B, are produced by Sinopec catalyzer branch office Chang Ling catalyst plant.The agent of hydrogenation diasphaltene and hydrofining agent are prepared by laboratory, and physico-chemical property is in table 2.The catalytic cracking catalyst that catalytic cracking unit uses is produced by catalyzer branch office of China Petrochemical Industry Shandong catalyst plant, and trade names are MLC-500.
Embodiment 1
Catalytic cracking heavy oil contacts with hydrofining agent with hydrogenation protecting agent, the agent of hydrogenation diasphaltene successively after mixing with hydrogen and reacts.Catalytic cracking heavy oil hydrogenation process conditions and generation oil nature are in table 3.The processing condition of catalytic cracking unit, product slates and gained gasoline property are in table 4.From table 3 and table 4, catalytic cracking heavy oil is after hydrotreatment, generating oily Δ H (hydrogen richness increase) is 1.50%, naphthene content is 45.0 % by weight, the propene yield that hydrogenated oil obtains through catalytic cracking is again 6.25%, yield of gasoline is 57.90%, and the octane value (RON) of gasoline is 93.6.
Comparative example 1
React with the catalyst exposure identical with embodiment 1 after catalytic cracking heavy oil and hydrogen mix.Catalytic cracking heavy oil hydrogenation process conditions and generation oil nature are in table 3.The processing condition of catalytic cracking unit, product slates and gasoline property are in table 4.From table 3 and table 4, catalytic cracking heavy oil is after hydrotreatment, generating oily Δ H (hydrogen richness increase) is 1.27%, naphthene content is 39.2 % by weight, the propene yield that hydrogenated oil obtains through catalytic cracking is again 4.32%, yield of gasoline is 53.20%, and gasoline octane rating (RON) is 91.1.
Comparative example 2
React with the catalyst exposure identical with embodiment 1 after catalytic cracking heavy oil and hydrogen mix.Catalytic cracking heavy oil hydrogenation process conditions and generation oil nature are in table 3.The processing condition of catalytic cracking unit, product slates and gasoline property are in table 4.From table 3 and table 4, catalytic cracking heavy oil is after hydrotreatment, generating oily Δ H (hydrogen richness increase) is 1.72%, naphthene content is 43.1 % by weight, the propene yield that hydrogenated oil obtains through catalytic cracking is again 4.25%, yield of gasoline is 58.50%, and the octane value (RON) of gasoline is 91.8.
By above embodiment and comparative example explanation, hydrogenation severity is controlled in rational interval by adjusting process condition, can under as far as possible low hydrogen consumption condition, obtain the hydrogenated oil that naphthene content is higher, again through catalytic cracking unit, can obtain more propylene and gasoline products, and the octane value of gasoline products is high.
Table 1
| Density (20 DEG C), g/cm 3 | 0.951 |
| Sulphur, heavy % | 0.68 |
| Nitrogen, heavy % | 0.14 |
| Hydrogen, heavy % | 10.85 |
| Mass spectrum quality forms, heavy % | |
| Paraffinic hydrocarbons | 13.5 |
| Naphthenic hydrocarbon | 27.8 |
| Mononuclear aromatics | 15.8 |
| Polycyclic aromatic hydrocarbons | 37.5 |
| Total aromatic hydrocarbons | 53.3 |
| Colloid | 5.4 |
| Gross weight | 100 |
Table 2
| Catalyzer | The agent of hydrogenation diasphaltene | Hydrofining agent |
| Chemical constitution, % by weight | ||
| Nickel oxide | 1.1 | 2.8 |
| Molybdenum oxide | 6.2 | |
| Tungsten oxide 99.999 | 26.2 | |
| Physical properties: | ||
| Specific surface area, m 2/g | 120 | 170 |
| Pore volume, ml/g | 0.71 | 0.33 |
| Crushing strength, N/mm | 11 | 18 |
| Shape | Butterfly-type | Butterfly-type |
Table 3
| Embodiment 1 | Comparative example 1 | Comparative example 2 | |
| Catalytic cracking heavy oil hydrogenation unit | |||
| Hydrogen dividing potential drop, MPa | 13.0 | 12.0 | 16.0 |
| Temperature, DEG C | 380 | 360 | 375 |
| Volume space velocity, h -1 | 0.60 | 1.20 | 0.50 |
| Hydrogen to oil volume ratio | 700 | 400 | 1000 |
| Catalytic cracking heavy oil character after hydrogenation | |||
| Density (20 DEG C), g/cm 3 | 0.9119 | 0.9219 | 0.9078 |
| Sulphur, μ g/g | 167 | 512 | 110 |
| Nitrogen, μ g/g | 109 | 235 | 83 |
| Hydrogen, heavy % | 12.35 | 12.12 | 12.57 |
| Δ H, heavy % | 1.50 | 1.27 | 1.72 |
| Mass spectrum quality forms, heavy % | |||
| Paraffinic hydrocarbons | 13.5 | 13.5 | 19.5 |
| Naphthenic hydrocarbon | 45.0 | 39.2 | 43.1 |
| Mononuclear aromatics | 21.7 | 25.1 | 21.6 |
| Polycyclic aromatic hydrocarbons | 19.8 | 22.2 | 15.8 |
| Total aromatic hydrocarbons | 41.5 | 47.3 | 37.4 |
| Colloid | 0 | 0 | 0 |
| Gross weight | 100 | 100 | 100 |
Table 4
| Embodiment 1 | Comparative example 1 | Comparative example 2 | |
| Catalytic cracking unit | |||
| Temperature of reaction, DEG C | 510 | 510 | 510 |
| Agent oil quality ratio | 5 | 5 | 5 |
| Weight hourly space velocity, h -1 | 10 | 10 | 10 |
| Catalytic cracking product distributes, heavy % | |||
| In gas | 1.75 | 1.78 | 1.72 |
| Liquefied gas | 14.11 | 12.18 | 17.35 |
| Wherein: propylene | 6.25 | 4.32 | 4.25 |
| Gasoline | 57.90 | 53.20 | 58.50 |
| Diesel oil | 15.1 | 19.21 | 13.12 |
| Heavy oil | 6.80 | 7.02 | 6.11 |
| Coke | 4.34 | 6.61 | 3.2 |
| Add up to | 100 | 100 | 100 |
| Total liquid yield, heavy % | 87.11 | 84.59 | 88.97 |
| Catalytically cracked gasoline character | |||
| Density (20 DEG C), g/cm3 | 0.730 | 0.730 | 0.730 |
| RON | 93.6 | 91.1 | 91.8 |
Claims (9)
1. produce the method for propylene and stop bracket gasoline for one kind, it is characterized in that, catalytic cracking heavy oil from catalytic cracking unit enters hydrogenation unit, contact with hydrogenation catalyst under hydrogenation conditions and react, the hydrogenated oil of gained enters catalytic cracking unit and carries out cracking reaction further, obtain object product propylene and gasoline, by controlling the hydrogenation severity of hydrogenation unit, make catalytic cracking heavy oil after hydrotreatment, 10 % by weight ~ 80 % by weight hydrotreated lube base oil of contained polycyclic aromatic hydrocarbons are naphthenic hydrocarbon; In catalytic cracking heavy oil and hydrogenated oil, the change of hydrogen richness is as the parameter characterizing hydrogenation severity; described hydrogenation catalyst be according to incoming flow to; the hydrogenation protecting agent of loading successively, the agent of hydrogenation diasphaltene and hydrofining agent; with hydrogenation unit integer catalyzer volume for benchmark; the admission space percentage ratio of described hydrogenation protecting agent, the agent of hydrogenation diasphaltene and hydrofining agent is respectively 2% ~ 30%, 5% ~ 50% and 5% ~ 93%.
2. in accordance with the method for claim 1, it is characterized in that, described catalytic cracking heavy oil refers to that catalytic cracking feeds is converted into unconverted part outside gas, gasoline, diesel oil and coke in catalytic cracking unit, and the boiling range of described catalytic cracking heavy oil is 260 DEG C ~ 550 DEG C.
3. in accordance with the method for claim 1, it is characterized in that, in catalytic cracking heavy oil, polycyclic aromatic hydrocarbon content is greater than 30 % by weight.
4. in accordance with the method for claim 1, it is characterized in that, in catalytic cracking heavy oil, polycyclic aromatic hydrocarbon content is greater than 35 % by weight.
5. in accordance with the method for claim 1, it is characterized in that, the reaction conditions of described hydrogenation unit is: hydrogen dividing potential drop 5.0MPa ~ 19.0MPa, temperature of reaction 330 DEG C ~ 410 DEG C, hydrogen to oil volume ratio 100Nm
3/ m
3~ 1800Nm
3/ m
3, volume space velocity 0.2h
-1~ 1.8h
-1.
6. in accordance with the method for claim 1, it is characterized in that, the reaction conditions of described hydrogenation unit is: hydrogen dividing potential drop 6.0MPa ~ 18.0MPa, temperature of reaction 340 DEG C ~ 400 DEG C, hydrogen to oil volume ratio 200Nm
3/ m
3~ 1200Nm
3/ m
3, volume space velocity 0.3h
-1~ 1.5h
-1.
7. in accordance with the method for claim 1; it is characterized in that; described hydrogenation protecting agent is Raschig ring shape; containing molybdenum on this alumina supporter of a kind of alumina supporter and load and/or tungsten; and nickel and/or cobalt, with the gross weight of hydrogenation protecting agent for benchmark, and with oxide basis; the content of molybdenum and/or tungsten is 1 ~ 10 % by weight, and the content of nickel and/or cobalt is 0.5 ~ 3 % by weight.Described aluminum oxide is gama-alumina, and the pore volume of described hydrogenation protecting agent is not less than 0.50ml/g.
8. in accordance with the method for claim 1, it is characterized in that, described hydrogenation diasphaltene agent is butterfly-type, containing a kind of carrier and load molybdenum on this carrier and/or tungsten, and nickel and/or cobalt, with the gross weight of hydrogenation diasphaltene agent for benchmark, and with oxide basis, the content of molybdenum and/or tungsten is 0.5 ~ 18 % by weight, the content of nickel and/or cobalt is 0.3 ~ 10 % by weight, carrier is aluminum oxide and optional silicon oxide, and described hydrogenation diasphaltene agent pore volume is not less than 0.60ml/g.
9. in accordance with the method for claim 1, it is characterized in that, described hydrofining agent is butterfly-type, containing a kind of carrier and load molybdenum on this carrier and/or tungsten, and nickel and/or cobalt, with the gross weight of hydrofining agent for benchmark, and with oxide basis, the content of molybdenum and/or tungsten is 10 ~ 40 % by weight, the content of nickel and/or cobalt is 0.3 ~ 7 % by weight, carrier is aluminum oxide and optional silicon oxide, and hydrofining agent pore volume is not less than 0.25ml/g.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103289741B (en) * | 2013-06-25 | 2015-04-15 | 中石化南京工程有限公司 | A combined method of hydrotreating-catalytic cracking-PSA purification for heavy oil |
| CN104342204B (en) * | 2013-07-30 | 2016-08-10 | 中国石油化工股份有限公司 | A kind of catalysis conversion method producing high-knock rating gasoline |
| CN105154135B (en) * | 2015-08-12 | 2017-05-17 | 中国石油大学(华东) | Method for producing aromatic hydrocarbon to the maximum from heavy oil |
| CN109423335B (en) * | 2017-08-30 | 2021-07-09 | 中国石油化工股份有限公司 | Catalytic cracking method for increasing gasoline yield |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101531923A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and high-octane gasoline |
| CN102108307A (en) * | 2009-12-24 | 2011-06-29 | 中国石油化工股份有限公司 | Method for lowering contents of impurities and polycyclic aromatic hydrocarbons in catalytic-cracking heavy oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101531923A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and high-octane gasoline |
| CN102108307A (en) * | 2009-12-24 | 2011-06-29 | 中国石油化工股份有限公司 | Method for lowering contents of impurities and polycyclic aromatic hydrocarbons in catalytic-cracking heavy oil |
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