CN103160317A - Production method of propylene and gasoline with high-octane rating - Google Patents
Production method of propylene and gasoline with high-octane rating Download PDFInfo
- Publication number
- CN103160317A CN103160317A CN2011104195467A CN201110419546A CN103160317A CN 103160317 A CN103160317 A CN 103160317A CN 2011104195467 A CN2011104195467 A CN 2011104195467A CN 201110419546 A CN201110419546 A CN 201110419546A CN 103160317 A CN103160317 A CN 103160317A
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- catalytic cracking
- agent
- oil
- weight
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- 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
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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, is a kind of by hydrogenation unit and catalytic cracking unit associating, the method that the processing catalytic cracking heavy oil is produced propylene and stop bracket gasoline.
Background technology
International oil price continues soaringly in recent years, and China's Economic development constantly increases the petroleum products demand of high value, the aggravation of contradictions of existing market to the lasting heaviness of the continuous lighting of petroleum products, high quality and the requirement that cleans and oil supply and in poor quality.Therefore promote the limited heavy oil resource 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 simultaneously the Main Means of producing propylene.In the U.S., almost 50% of the propylene market demand all derive from catalytic cracking unit.Transformation efficiency and the yield of light oil of existing catalytic cracking unit in order to increase catalytic cracking, usually the heavy oil that catalytic unit is produced (heavy cycle oil) self circulates in catalytic cracking unit, 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, has increased the For Fcc Regenerator load, has reduced treatment capacity and the petrol and diesel oil product yield of catalytic cracking unit.
CN101531923A has proposed 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 that obtains obtains propylene, gasoline, catalytic cracking heavy oil and other product through catalytic cracking, and wherein catalytic cracking heavy oil enters hydrotreater; Catalytic cracking heavy oil after hydrogenation is circulated to the further reaction of catalytic cracking unit and obtains purpose product propylene and gasoline.
Summary of the invention
The objective of the invention is on the basis of existing technology, a kind of method of hydrotreatment and catalytic cracking combination is provided, produce 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 further carries out cracking reaction, obtain purpose product propylene and gasoline, by controlling the hydrogenation severity of hydrogenation unit, make catalytic cracking heavy oil after hydrotreatment, 10 % by weight of contained polycyclic aromatic hydrocarbons～80 % by weight hydrogenation are saturated is naphthenic hydrocarbon.Catalytic cracking heavy oil contacts with hydrogenation catalyst with the hydrogen mixing and reacts.
Described catalytic cracking heavy oil refers to that the catalytic cracking charging 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 ℃～550 ℃.The catalytic cracking heavy oil aromaticity content is high, and is mainly polycyclic aromatic hydrocarbons, and wherein polycyclic aromatic hydrocarbon content greater than 30 % by weight, is preferably greater than 35 % by weight.
In the method catalytic cracking heavy oil is after hydrotreatment, the saturated generation naphthenic hydrocarbon of part polycyclic aromatic hydrocarbons hydrogenation wherein, and naphthenic hydrocarbon can be produced propylene and stop bracket gasoline through further catalytic cracking.Therefore in hydrogenated oil, the content of naphthenic hydrocarbon is higher, more is conducive to produce 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 discharging of revivifier SOx.Because nitrogen compound can make the active centre of acidic catalyst cracking catalyst poisoning, activity decreased, transformation efficiency descends, so the reduction of nitrogen content can improve transformation efficiency and the product yield of catalytic cracking heavy oil.
The present invention with the variation of hydrogen richness in catalytic cracking heavy oil and hydrogenated oil as the parameter that characterizes the hydrogenation severity.The inventor finds by research, and in the catalytic cracking heavy oil hydrogenated oil, the content of mononuclear aromatics is associated with the hydrogenation severity.With the variation (Δ H) of hydrogen richness before and after a catalytic cracking heavy oil hydrogenation parameter as sign 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 due to the saturated naphthenic hydrocarbon that generated of polycyclic aromatic hydrocarbons hydrogenation.When the hydrogenation severity was increased to a degree, the naphthene content in hydrogenated oil no longer increased, and this is mainly owing to there being the hydrocracking of part naphthenic hydrocarbon to generate paraffinic hydrocarbons.If further improve the hydrogenation severity, the hydrogen of consumption will be mainly used in hydrocracking reaction again, rather than the hydrogenation saturated reaction of polycyclic aromatic hydrocarbons.Hydrogen is one of main cost of hydrotreatment process.Therefore to control the hydrogenation severity in the hydrotreatment process of catalytic cracking heavy oil in a rational interval (dash area in figure), so just can obtain the highest hydrogenated oil of naphthene content under the condition that consumes the hydrogen of trying one's best less.The control of hydrogenation severity can realize by the 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, 330 ℃～410 ℃ of temperature of reaction, preferred 340 ℃～400 ℃, 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; hydrogenation protecting agent, the agent of hydrogenation diasphaltene and the hydrofining agent of filling successively; take hydrogenation unit integer catalyzer volume as benchmark; the admission space percentage ratio of described hydrogenation protecting agent, the agent of hydrogenation diasphaltene and hydrofining agent is respectively 2%～30%, and 5%～50% and 5%～93%.
Described hydrogenation protecting agent is the Raschig ring shape; contain a kind of alumina supporter and the molybdenum and/or the tungsten that load on this alumina supporter; and nickel and/or cobalt; take the gross weight of hydrogenation protecting agent as benchmark; and in oxide compound; 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, preferably is 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 is in the larger hydrogenation protecting agent of the top of reactor filling voidage; can further remove the tiny catalytic cracking catalyst powder of carrying secretly in raw material; the foulant of easy green coke in while energy effective elimination raw material; reach the purpose of protection hydrogenation Primary Catalysts, guarantee the hydrotreater long-time running.
The agent of described hydrogenation diasphaltene is the butterfly type, contain a kind of carrier and the molybdenum and/or the tungsten that load on this carrier, and nickel and/or cobalt, take the gross weight of hydrogenation diasphaltene agent as benchmark, and in oxide compound, 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, preferably is 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 in 3000 μ g/g left and right, far above the requirement of conventional Wax Oil Hydrogenation Unit design charging.And, bituminous matter is component the heaviest in catalytic cracking heavy oil, is green coke precursor main in catalytic cracking heavy oil, and molecular dimension often reaches tens more than nanometer, easily cause the catalyzer coking and deactivation, affect the work-ing life of catalyst activity stability and shortening catalyzer.Therefore the hydrogenation diasphaltene agent that will load large pore volume in hydrogenation protecting agent back makes bituminous matter in raw material can obtain part and removes, to reach the purpose of protection rear portion hydrofining agent.
Described hydrofining agent is the butterfly type, contain a kind of carrier and the molybdenum and/or the tungsten that load on this carrier, and nickel and/or cobalt, take the gross weight of hydrofining agent as benchmark, and in oxide compound, 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, preferably is not less than 0.30ml/g.At hydrogenation diasphaltene catalyzer back filling Hydrobon catalyst, this catalyzer has much higher Polycyclic aromatic hydrocarbons saturated activity, has simultaneously high desulfurization and denitrification activity.
In the present invention, catalytic cracking unit can be a cover or an above catalytic cracking unit of cover, and every covering device should comprise a reactor, a revivifier and a separation column at least.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 to be referred as agent-oil ratio) 3～10 of 470 ℃～570 ℃ of temperature of reaction, 0.5 second～5 seconds reaction times, catalyzer and stock oil, 650 ℃～800 ℃ of regeneration temperatures.
Advantage of the present invention is:
(1), the present invention can improve the cracking performance of catalytic cracking heavy oil greatly, thereby improved catalytic cracking unit transformation efficiency and yield of light oil, realize the efficient utilization of petroleum resources.
(2), the present invention controls the hydrogenation severity in rational interval by adjusting catalytic cracking heavy oil hydrogenation technique condition, the hydrogenated oil of naphthenic hydrocarbon be can obtain being rich in, and more propylene and high-octane gasoline products obtained by follow-up catalytic cracking process.
Description of drawings
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 that adopts in embodiment sees Table 1.The filling ratio of the hydrogenation protecting agent that the 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 the laboratory, and physico-chemical property sees Table 2.The catalytic cracking catalyst that catalytic cracking unit uses is by the Shandong catalyst plant production of catalyzer branch office of China Petrochemical Industry, and trade names are MLC-500.
Embodiment 1
Contact with the hydrofining agent with hydrogenation protecting agent, the agent of hydrogenation diasphaltene successively after catalytic cracking heavy oil and hydrogen mix and react.Catalytic cracking heavy oil hydrogenation technique condition and generation oil nature see Table 3.The processing condition of catalytic cracking unit, product distribute and the gained gasoline property sees Table 4.By table 3 and as seen from 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 again is 6.25%, yield of gasoline is 57.90%, and the octane value of gasoline (RON) is 93.6.
Comparative Examples 1
The catalyzer that catalytic cracking heavy oil is rear and identical with embodiment 1 with the hydrogen mixing contacts and reacts.Catalytic cracking heavy oil hydrogenation technique condition and generation oil nature see Table 3.The processing condition of catalytic cracking unit, product distribute and gasoline property sees Table 4.By table 3 and as seen from 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 again is 4.32%, yield of gasoline is 53.20%, and gasoline octane rating (RON) is 91.1.
Comparative Examples 2
The catalyzer that catalytic cracking heavy oil is rear and identical with embodiment 1 with the hydrogen mixing contacts and reacts.Catalytic cracking heavy oil hydrogenation technique condition and generation oil nature see Table 3.The processing condition of catalytic cracking unit, product distribute and gasoline property sees Table 4.By table 3 and as seen from 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 again is 4.25%, yield of gasoline is 58.50%, and the octane value of gasoline (RON) is 91.8.
By above embodiment and Comparative Examples explanation, control the hydrogenation severity in rational interval by the adjusting process condition, can be under the hydrogen consumption condition of trying one's best low, obtain the higher hydrogenated oil of naphthene content, 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 ℃), g/cm 3 | 0.951 |
| Sulphur, heavy % | 0.68 |
| Nitrogen, heavy % | 0.14 |
| Hydrogen, heavy % | 10.85 |
| The 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 | The 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 | The butterfly type | The butterfly type |
Table 3
| Embodiment 1 | Comparative Examples 1 | Comparative Examples 2 | |
| The catalytic cracking heavy oil hydrogenation unit | |||
| The hydrogen dividing potential drop, MPa | 13.0 | 12.0 | 16.0 |
| Temperature, ℃ | 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 ℃), 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 |
| The 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 Examples 1 | Comparative Examples 2 | |
| Catalytic cracking unit | |||
| Temperature of reaction, ℃ | 510 | 510 | 510 |
| Agent oil quality ratio | 5 | 5 | 5 |
| Weight hourly space velocity, h -1 | 10 | 10 | 10 |
| The 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 ℃), g/cm3 | 0.730 | 0.730 | 0.730 |
| RON | 93.6 | 91.1 | 91.8 |
Claims (11)
1. method of producing propylene and stop bracket gasoline, 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 further carries out cracking reaction, obtain purpose product propylene and gasoline, by controlling the hydrogenation severity of hydrogenation unit, make catalytic cracking heavy oil after hydrotreatment, 10 % by weight of contained polycyclic aromatic hydrocarbons～80 % by weight hydrogenation are saturated is naphthenic hydrocarbon.
2. in accordance with the method for claim 1, it is characterized in that, described catalytic cracking heavy oil refers to that the catalytic cracking charging 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 ℃～550 ℃.
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, with the variation of hydrogen richness in catalytic cracking heavy oil and hydrogenated oil as the parameter that characterizes the hydrogenation severity.
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 5.0MPa～19.0MPa, 330 ℃～410 ℃ of temperature of reaction, hydrogen to oil volume ratio 100Nm
3/ m
3～1800Nm
3/ m
3, volume space velocity 0.2h
-1～1.8h
-1
7. 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, 340 ℃～400 ℃ of temperature of reaction, hydrogen to oil volume ratio 200Nm
3/ m
3～1200Nm
3/ m
3, volume space velocity 0.3h
-1～1.5h
-1
8. in accordance with the method for claim 1; it is characterized in that; described hydrogenation catalyst comprise according to incoming flow to; hydrogenation protecting agent, the agent of hydrogenation diasphaltene and the hydrofining agent of filling successively; take hydrogenation unit integer catalyzer volume as benchmark; the admission space percentage ratio of described hydrogenation protecting agent, the agent of hydrogenation diasphaltene and hydrofining agent is respectively 2%～30%, and 5%～50% and 5%～93%.
9. in accordance with the method for claim 1; it is characterized in that; described hydrogenation protecting agent is the Raschig ring shape; contain a kind of alumina supporter and the molybdenum and/or the tungsten that load on this alumina supporter; and nickel and/or cobalt, take the gross weight of hydrogenation protecting agent as benchmark, and in oxide compound; 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.
10. in accordance with the method for claim 1, it is characterized in that, the agent of described hydrogenation diasphaltene is the butterfly type, contains a kind of carrier and the molybdenum and/or the tungsten that load on this carrier, and nickel and/or cobalt, take the gross weight of hydrogenation diasphaltene agent as benchmark, and in oxide compound, the content of molybdenum and/or tungsten is 0.5～18 % by weight, and 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.
11. in accordance with the method for claim 1, it is characterized in that, described hydrofining agent is the butterfly type, contains a kind of carrier and the molybdenum and/or the tungsten that load on this carrier, and nickel and/or cobalt, take the gross weight of hydrofining agent as benchmark, and in oxide compound, the content of molybdenum and/or tungsten is 10～40 % by weight, and 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110419546.7A CN103160317B (en) | 2011-12-15 | 2011-12-15 | Production method of propylene and gasoline with high-octane rating |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110419546.7A CN103160317B (en) | 2011-12-15 | 2011-12-15 | Production method of propylene and gasoline with high-octane rating |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103160317A true CN103160317A (en) | 2013-06-19 |
| CN103160317B CN103160317B (en) | 2015-07-01 |
Family
ID=48583856
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110419546.7A Active CN103160317B (en) | 2011-12-15 | 2011-12-15 | Production method of propylene and gasoline with high-octane rating |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103160317B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103289741A (en) * | 2013-06-25 | 2013-09-11 | 中石化南京工程有限公司 | A combined method of hydrotreating-catalytic cracking-PSA purification for heavy oil |
| CN104342204A (en) * | 2013-07-30 | 2015-02-11 | 中国石油化工股份有限公司 | Catalytic conversion method for producing high-octane gasoline |
| CN105154135A (en) * | 2015-08-12 | 2015-12-16 | 中国石油大学(华东) | Method for producing aromatic hydrocarbon to the maximum from heavy oil |
| CN109423335A (en) * | 2017-08-30 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of catalyst cracking method of fecund gasoline |
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 |
-
2011
- 2011-12-15 CN CN201110419546.7A patent/CN103160317B/en active Active
Patent 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 |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103289741A (en) * | 2013-06-25 | 2013-09-11 | 中石化南京工程有限公司 | A combined method of hydrotreating-catalytic cracking-PSA purification for heavy oil |
| CN104342204A (en) * | 2013-07-30 | 2015-02-11 | 中国石油化工股份有限公司 | Catalytic conversion method for producing high-octane gasoline |
| 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 |
| CN105154135A (en) * | 2015-08-12 | 2015-12-16 | 中国石油大学(华东) | Method for producing aromatic hydrocarbon to the maximum from heavy oil |
| 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 |
| CN109423335A (en) * | 2017-08-30 | 2019-03-05 | 中国石油化工股份有限公司 | A kind of catalyst cracking method of fecund gasoline |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103160317B (en) | 2015-07-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101519603B (en) | Method for hydrotreating high-sulfur and high-metal residual oil | |
| CN103121897B (en) | By the method for the mixture preparing aromatic hydrocarbon containing hydrocarbon with condensed rings | |
| CN105647573A (en) | Method for producing light-weight aromatic hydrocarbons and clean fuel oil by moving bed hydrocracking | |
| CN102344828B (en) | Processing method of inferior residual oil | |
| CN103059986B (en) | Hydrocracking method for producing chemical materials | |
| CN1952069A (en) | Combined hydrogenation method | |
| CN112745922B (en) | Hydrocracking method for poor-quality diesel raw material | |
| CN103160317B (en) | Production method of propylene and gasoline with high-octane rating | |
| CN107557064B (en) | Coal tar combined bed hydrogenation method and system for coal tar combined bed hydrogenation | |
| CN103071527B (en) | A kind of method for hydrogen cracking preparing high-octane naphtha | |
| CN102634368B (en) | Method for modifying inferior gasoline | |
| CN102344829B (en) | Combination method for residue hydrotreatment, catalytic cracking heavy oil hydrogenation and catalytic cracking | |
| CN113817503B (en) | Combined process for preparing chemical products from crude oil | |
| CN114437803B (en) | Hydrotreatment method of catalytic diesel | |
| CN114437802B (en) | Hydrotreating method of full fraction catalytic diesel oil | |
| CN114437795A (en) | Method and system for processing heavy oil | |
| CN102757819B (en) | Method of using catalytic cracking heavy oil to produce high-octane gasoline | |
| CN103059941B (en) | Prepare the method for hydrogen cracking of high-octane naphtha | |
| CN103059993A (en) | Catalytic conversion method of petroleum hydrocarbon | |
| CN116410793B (en) | Combined processing method of light diesel oil | |
| CN101724447B (en) | Method for producing gasoline blend component with high octane value by using cracking gasoline heavy fractions | |
| CN103059992B (en) | Effective catalytic conversion method of petroleum hydrocarbon | |
| CN102373086A (en) | Method using gas oil and residual oil to process light fuel | |
| CN109988630B (en) | Wax oil hydrogenation method and system | |
| CN107557068B (en) | Coal tar hydrogenation method and system for coal tar hydrogenation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |