CN101987971B - Method for producing high-octane petrol by inferior diesel - Google Patents
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Abstract
The invention relates to a method for producing high-octane petrol by inferior diesel. A mixture of diesel raw oil and hydrogen gas reacts with a hydrorefining catalyst in a first reaction zone and a hydrocracking catalyst in a second reaction zone in sequence, the saturation depth of arene in the first reaction zone is controlled, i.e. compared with diesel raw oil, the saturation ratio of two-ring and more than two-ring arene in reaction effluent of the first reaction zone is more than 50%, and taking the liquid components of the reaction effluent of the first reaction zone as a reference, the content of single-ring arene is increased to more than 40% by mass. Low-sulfur high-octane petrol can be produced from inferior diesel fractions with high arene content by using the single-pass process flow and a method of properly controlling reaction depth, and meanwhile, a low-sulfur clean diesel blend component can also be produced.
Description
Technical field
The present invention relates to a kind of is the hydrocarbon ils cleavage method that obtains low boiler cut in the situation that there is hydrogen, more particularly, is a kind of method of being produced stop bracket gasoline by poor ignition quality fuel.
Background technology
Along with the development of crude oil heaviness and the rapid growth of market to light-end products demand, in China, as the working ability development of the catalytic cracking technology of light materialization of heavy oil major technique rapidly, China's catalyzed cracking processing ability accounts for 1/3rd left and right of crude oil time processing ability, at the forefront in the world.Yet along with the raising of catalyzed cracking processing ability, the output of China's catalytic diesel oil increases year by year, degradation, main manifestations is aromatic hydrocarbons, sulphur, nitrogen, olefin(e) centent is high, cetane value is low and stability is poor.Especially due to the difference of stock oil and catalytic cracking process, from 50 quality % to content 80 quality % not etc., the above aromaticity content of dicyclo and dicyclo is more than 40 quality % for total aromaticity content of catalytic cracking diesel oil.And this part catalytic diesel oil accounts for 1/3rd of Chinese commodity diesel oil share.Meanwhile, along with the continuous enhancing of people's environmental consciousness, environmental regulation has proposed more strict requirement to the quality of diesel oil, thereby causes great majority to take its diesel product of refinery that catalytic cracking technology is main processing technology being difficult to meet the requirement of market quality.In addition, the diesel oil of some non-petroleum base cuts, the diesel oil distillate of coal direct liquefaction oil or coal tar for example, because sulphur, nitrogen, aromaticity content height are also difficult to meet the requirement of market quality.Therefore, the oil product that is processed into high added value of poor ignition quality fuel is seemed to particularly important and urgent.
On the other hand, in current China gasoline pool, catalytic gasoline proportion is up to 78%, cause the alkene of gasoline high with sulphur content, aromaticity content is low, octane value is relative on the low side, therefore, market also needs to develop a kind of production technology of producing low-sulfur, clean gasoline with high octane.
The technique of poor ignition quality fuel production high added value oil product mainly contains hydrofining and hydrocracking two classes.Adopt conventional hydrofining technology to process poor ignition quality fuel, although can effectively remove the impurity such as sulphur in diesel oil, nitrogen, diesel product cetane value increase rate is limited, and diesel oil variable density is also little; Adopt traditional hydrocracking process processing poor ignition quality fuel, although can the good low-sulfur diesel-oil blend component of production product performance, need comparatively harsh reaction conditions, and its naphtha fraction yield is low.Although or can produce to greatest extent petroleum naphtha, and the naphtha fraction octane value of its production is lower, and its research octane number (RON) only has 75 left and right.
US 7,384, and 542B1 discloses a kind of method of producing low-sulfur diesel-oil and stop bracket gasoline.This patent enters hydrogenating desulfurization, hydrodenitrification reaction zone by straight-run diesel oil and/or light wax tailings (LCGO), catalytic cracking diesel oil (LCO) enters hydrocracking reaction district, the product of Liang Ge reaction zone enters cold high score, cold low minute after mixing, then enter fractionating system separation and obtain high-octane number component and low-sulfur diesel-oil.In this invention, hydrocracking reaction district adopts hydrocracking catalyst amorphous or that contain low molecular sieve level.This invention can be processed straight-run diesel oil and/or LCGO, and the LCO of 149～343 ℃ of parts, 88～193 ℃ of heavy naphtha fraction octane values 87 that obtain, and 193 ℃ of sulphur content of diesel fraction of > are less than 10ppm, cetane index 46.
US 4,985, disclose a kind of technique of producing stop bracket gasoline in 134.This invention raw material boiling spread is the LCO of 150～327 ℃, i.e. light constituent in catalytic cracking light cycle oil.The hydrocracking catalyst adopting contains Y zeolite, USY molecular sieve or dealuminzation Y zeolite.In addition, in fractionation product oil, be greater than gasoline fraction and be less than 232 ℃ or be less than the middle runnings of 260 ℃ and be back to hydrocracking reactor entrance or be back to catalytic cracking reaction zone.
Summary of the invention
The object of the invention is to provide on the basis of existing technology a kind of method of being produced stop bracket gasoline by poor ignition quality fuel.Specifically, be will solve prior art processing poor ignition quality fuel and produce gasoline time, poor ignition quality fuel raw material is done low, and the problem such as gained gasoline products octane value is low.
Method provided by the invention, comprise: diesel raw material oil-hydrogen mixture is first in the first reaction zone and Hydrobon catalyst contact reacts, the reaction effluent of the first reaction zone enters second reaction zone and hydrocracking catalyst contact reacts without separation, the reaction effluent of second reaction zone is through cooling, after separation, obtain hydrogen-rich gas and product liquid, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is more than 50%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, more than its mononuclear aromatics content is increased to 40 quality %.
In the first ，Ji hydrofining reaction district, reaction zone, poor ignition quality fuel raw material mainly carries out the reactions such as hydrogenating desulfurization, hydrodenitrification and aromatic saturation.In the present invention, pass through to control the degree of depth of hydrofining reaction process, impel the above aromatic saturation of dicyclo and dicyclo to become mononuclear aromatics, avoiding supersaturation is naphthenic hydrocarbon, in reducing diesel oil in the foreign matter content such as sulphur, nitrogen, reduce dicyclo and the above aromaticity content of dicyclo, and increase mononuclear aromatics content.In second reaction zone, Ji hydrocracking reaction district, liquid ingredient in the reaction effluent of the first reaction zone (hydrofining product oil) carries out selective opening on hydrogenation-cracking function catalyzer, the reactions such as cracking, effectively make short-side chain alkylbenzene, the mononuclear aromatics side chain selectivity that the cetane value such as naphthane are low is carried out open loop, the reactions such as cracking, impel more micromolecular mononuclear aromatics in diesel oil distillate to be converted into the benzene in gasoline fraction, the high-octane number components such as toluene, thereby reach, improve gasoline fraction product hydrocarbon composition, improve the object of gasoline fraction product octane value.Retain as far as possible more macromolecular long chain alkane in diesel oil distillate or with high hexadecane value components such as the naphthenic hydrocarbon of long side chain or aromatic hydrocarbons simultaneously, thereby reach raising diesel product cetane value, improve the object of product diesel quality.
In another preferred version of the present invention, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is more than 60%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, more than its mononuclear aromatics content is increased to 50 quality %.
The present invention adopts a through type technical process of conventional hydrofining-hydrocracking, and without separated in the middle of any, device flow process is simple, and easy handling, can utilize existing device to transform, and investment and the process cost of equipment are lower.Described one-pass technical process Zhong， hydrofining reaction district and hydrocracking reaction district can be arranged in a reactor, also can be arranged in two reactors.
The boiling spread of diesel raw material oil of the present invention is 165～400 ℃, and total aromaticity content is higher than 65 quality %, and preferably total aromaticity content is 65～90 quality %, and wherein the content of dicyclo and the above aromatic hydrocarbons of dicyclo is higher than 40 quality %, preferably 40～65 quality %.Described diesel raw material grease separation catalytic cracking light cycle oil, heavy catalytic cycle oil, the straight-run diesel oil of naphthenic base crude, the diesel oil distillate of the coker gas oil of naphthenic base crude, coal direct liquefaction oil are, one or more in the diesel oil distillate of coal tar.
The first described reaction zone and the reaction conditions of second reaction zone are: hydrogen dividing potential drop 3.0～10.0MPa, preferred 4.0～6.5MPa, 300～450 ℃ of temperature of reaction, preferably 350～430 ℃, hydrogen to oil volume ratio 400～1600Nm
3/ m
3, preferred 500～1200Nm
3/ m
3, volume space velocity 0.2～2.5h during liquid
-1, preferred 0.4～1.5h
-1.
Hydrobon catalyst in the first described reaction zone and the loadings of the hydrocracking catalyst in second reaction zone are to determine according to the nitrogen content of processed stock oil.When diesel raw material oil nitrogen content is that 700 μ g/g-2000 μ g/g are when above, Hydrobon catalyst is 5: 1～1: 5 with hydrocracking catalyst admission space ratio, be preferably 3: 1～1: 1, when diesel raw material oil nitrogen content is less than 700 μ g/g, Hydrobon catalyst is 1: 1～1: 5 with hydrocracking catalyst admission space ratio, is preferably 1: 1～1: 2.
If carbon residue or metal content are higher in stock oil; for preventing that the Pressure Drop of beds from reaching limit value too quickly; can load respectively at Hydrobon catalyst bed top the hydrogenation protecting agent that accounts for hydrofining agent volume total amount 5～20%, to protect Primary Catalysts, to avoid the quick coking of bed.Protective material is comprised of the gamma-aluminium oxide carrier with diplopore distribution of 1.0～5.0 heavy % nickel oxide, 5.5～10.0 heavy % molybdenum oxides and surplus.
Described Hydrobon catalyst is to load on composite alumina and/or combined oxidation silicon carrier Shang VIII family's base metal and/or group vib non-precious metal catalyst.Preferred Hydrobon catalyst consists of: in oxide compound and take catalyzer total amount as benchmark, the content of nickel and/or cobalt is 1～10 heavy %, and molybdenum and tungsten sum are greater than 10～50 heavy %, the heavy % of fluorine 1～10, and all the other are aluminum oxide and silicon oxide.This Hydrobon catalyst has good hydrogenating desulfurization, hydrodenitrification performance, and the aromatic saturation performance of part, in can the hydrotreatment for poor-quality diesel-oil by cut fraction, the impurity such as the sulphur in energy effective elimination raw material, nitrogen, and appropriateness is carried out aromatic saturation reaction, impel the above aromatic saturation of dicyclo and dicyclo to become mononuclear aromatics, avoiding supersaturation is naphthenic hydrocarbon.
Described hydrocracking catalyst is to load on complex carrier Shang VIII family's base metal and/or group vib non-precious metal catalyst, in oxide compound and take catalyzer total amount as benchmark, catalyzer mesolite content is the heavy % of 1-90, the heavy % of aluminum oxide 5-80, the heavy % of metal component 3～30 of the heavy % of group VIII metal component 1～15, group vib.Preferred hydrocracking catalyst has following composition: the heavy % of fluorine 0.5～5.0, the heavy % of nickel oxide 2.5～6.0, the heavy % of Tungsten oxide 99.999 10～38, all the other are carrier, zeolite in this carrier is the mixture of a kind of large pore zeolite and a kind of mesopore zeolite, in catalyzer, large pore zeolite weighs % containing 1～65 heavy %, mesopore zeolite containing 1-50.Described hydrocracking catalyst has good selective cracking function, this cracking catalyst has good selectivity to reactions such as the fracture of mononuclear aromatics side chain, naphthane selective opening and disconnected side chains, make the mononuclear aromatics generation selective cracking reaction in diesel oil distillate generate the high octane gasoline components such as benzene, toluene, thereby improve gasoline fraction hydrocarbon composition, increase the octane value of gasoline fraction.
The present invention adopts one-pass technical process, adopt the method for moderate control reaction depth, can be less than by the poor-quality diesel-oil by cut fraction production sulphur content of high aromaticity content 50 μ g/g, research octane number (RON) higher than 89 gasoline fraction, simultaneously can also production sulphur content be less than 50 μ g/g, actual measurement cetane value improves clean diesel blend component more than 10Ge unit compared with stock oil.In addition, the present invention has adopted a kind of hydrocracking reaction flow process of routine, easy handling, and facility investment is lower.
Accompanying drawing explanation
Accompanying drawing is the schematic flow sheet of being produced the method for stop bracket gasoline by poor ignition quality fuel provided by the invention.
Embodiment
Below in conjunction with accompanying drawing, method provided by the present invention is further detailed.Accompanying drawing is the schematic flow sheet of being produced stop bracket gasoline method by poor ignition quality fuel provided by the invention.In figure, omitted much equipment, as pump, interchanger, compressor etc., but this is known to those of ordinary skills.
The flow process of method provided by the invention is described in detail as follows: from the stock oil process raw oil pump 2 of pipeline 1, preheating is mixed into the first reactor 3 by pipeline 11 and hydrogen or hydrogen-rich gas from pipeline 10, contact with Hydrobon catalyst, carry out desulfurization, denitrogenation and the reaction of appropriate aromatic saturation.The reaction effluent of the first reactor 3 directly enters the second reactor 4 through pipeline 12 without separation in the middle of any and contacts with hydrocracking catalyst, carries out the cracking reaction of suitable selectivity side chain fracture.The reaction effluent of the second reactor 4 enters cold high pressure separator 5 through pipeline 13 and carries out gas-liquid separation, and separating obtained hydrogen-rich gas enters circulating hydrogen compressor 7 through pipeline 15, returns to the entrance of the first reactor 3 and the second reactor 4 through boosting by pipeline 10.The isolated liquid stream of cold high pressure separator 5 enters light pressure separator 6 through pipeline 14 and carries out further gas-liquid separation, and separating obtained gas is through pipeline 17 dischargers, and the product liquid of gained enters fractionating system 8 through pipeline 16 and carries out component cutting.Separated diesel oil distillate is extracted out through pipeline 18, and separated gasoline fraction is extracted out through pipeline 19.
The following examples will be further described the present invention, but not thereby limiting the invention.
In embodiment, the trade names of Hydrobon catalyst A are RN-10, the trade names of Hydrobon catalyst B are RS-1000, the trade names of hydrocracking catalyst C are RT-5, and all catalyzer are produced by China PetroChemical Corporation's Chang Ling catalyst plant.
In embodiment, stock oil D used and E are respectively from different catalytic cracking unit, and its character is listed in table 1.As can be seen from Table 1, more than total aromaticity content of stock oil D and E has all surpassed 75 quality %, the content of the dicyclo of stock oil D and the above aromatic hydrocarbons of dicyclo is up to 46.9 quality %, and cetane value is only 20.6, the content of the dicyclo of stock oil E and the above aromatic hydrocarbons of dicyclo is up to 58.6 quality %, and cetane value is less than 19.3, be the poor-quality diesel-oil by cut fraction of high aromaticity content.
Embodiment 1
Stock oil D enters hydrogenator together with hydrogen, successively with the Hydrobon catalyst B of the first reaction zone, the hydrocracking catalyst C contact reacts of second reaction zone, reacted effluent enters high-pressure separator without separation in the middle of any, light pressure separator, through refrigerated separation, hydrogen-rich gas recycles, product liquid enters fractionating system and is separated into gasoline fraction and diesel oil distillate, Hydrobon catalyst is 3: 2 with the admission space ratio of hydrocracking catalyst, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is 69.7%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, its mononuclear aromatics content is 51.6 quality %.Reaction conditions is as shown in table 2, and product yield and character are as shown in table 3.
As can be seen from Table 3, the yield of gasoline fraction product is 43.5 heavy %, sulphur content 32 μ g/g, gasoline fraction research octane number (RON) 91.4, motor-method octane number 80.9; The actual measurement cetane value of diesel oil distillate product is 30.9, compares with raw material, and cetane value improves 10.3 units, and sulphur content is less than 50 μ g/g.
Stock oil D enters hydrogenator together with hydrogen, successively with the Hydrobon catalyst A of the first reaction zone, the hydrocracking catalyst C contact reacts of second reaction zone, reacted effluent enters high-pressure separator without separation in the middle of any, light pressure separator, through refrigerated separation, hydrogen-rich gas recycles, product liquid enters fractionating system and is separated into gasoline fraction and diesel oil distillate, Hydrobon catalyst is 1: 1 with the admission space ratio of hydrocracking catalyst, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is 54.9%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, its mononuclear aromatics content is 52.5 quality %.Reaction conditions is as shown in table 2, and product yield and character are as shown in table 3.
As can be seen from Table 3, the yield of gasoline fraction product is 38.8 heavy %, sulphur content 38 μ g/g, gasoline fraction research octane number (RON) 89.4, motor-method octane number 80.5; The actual measurement cetane value of diesel oil distillate product is 30.6, compares with raw material, and cetane value improves 10Ge unit, and sulphur content is less than 50 μ g/g.
Stock oil E enters hydrogenator together with hydrogen, successively with the Hydrobon catalyst A of the first reaction zone, the hydrocracking catalyst C contact reacts of second reaction zone, reacted effluent enters high-pressure separator without separation in the middle of any, light pressure separator, through refrigerated separation, hydrogen-rich gas recycles, product liquid enters fractionating system and is separated into gasoline fraction and diesel oil distillate, Hydrobon catalyst is 2: 3 with the admission space ratio of hydrocracking catalyst, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is 55.0%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, its mononuclear aromatics content is 51.8 quality %.Reaction conditions is as shown in table 2, and product yield and character are as shown in table 3.
As can be seen from Table 3, the yield of gasoline fraction product is 49.0 heavy %, and sulphur content is less than 50 μ g/g, gasoline fraction research octane number (RON) 92.0, motor-method octane number 81.3; The actual measurement cetane value of diesel oil distillate product is 30.1, compares with raw material, and cetane value improves 10.8 units, and sulphur content is less than 50 μ g/g.
Table 1
| Stock oil | D | E |
| Density (20 ℃), g/cm 3 | 0.9340 | 0.9472 |
| Viscosity (20 ℃), mm 2/s | 5.115 | 4.831 |
| Bromine valency, gBr/100g | 10.8 | 13.2 |
| Refractive power, n D 20 | 1.5427 | 1.5523 |
| Sulphur, μ g/g | 7600 | 14000 |
| Nitrogen, μ g/g | 1075 | 455 |
| Cetane value | 20.6 | ＜19.3 |
| Total aromaticity content, quality % | 76.5 | 78.7 |
| The above aromaticity content of dicyclo, quality % | 46.9 | 58.6 |
| Boiling range (ASTM D-86), ℃ | ||
| Initial boiling point | 206 | 184 |
| 10％ | 231 | 224 |
| 50％ | 280 | 269 |
| Final boiling point | 365 | 372 |
Table 2
| Numbering | Embodiment 1 | |
|
| Stock oil | D | D | E |
| Hydrofining/hydrocracking catalyst | B/C | A/C | A/C |
| Reaction conditions | |||
| Hydrogen dividing potential drop, MPa | 5.5 | 4.5 | 5.0 |
| Temperature of reaction, ℃ | 360/400 | 380/390 | 360/410 |
| Cumulative volume air speed, h -1 | 1.0 | 0.8 | 1.0 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 700 | 800 | 900 |
Table 3
| Embodiment 1 | |
|
|
| Gasoline fraction character: | |||
| Yield, % by weight | 43.5 | 38.8 | 49.0 |
| Density (20 ℃), g/cm 3 | 0.7780 | 0.7840 | 0.7930 |
| Sulphur content, μ g/g | 32 | 38 | ＜50 |
| Research octane number (RON) | 91.4 | 89.4 | 92.0 |
| Motor-method octane number | 80.9 | 80.5 | 81.3 |
| Boiling range ASTM D-86, ℃ | |||
| IBP | 57 | 60 | 49 |
| 10％ | 70 | 72 | 69 |
| 50％ | 133 | 115 | 136 |
| FBP | 198 | 203 | 200 |
| Diesel oil distillate character: | |||
| Density (20 ℃), g/cm 3 | 0.8950 | 0.9010 | 0.9129 |
| Sulphur content, μ g/g | ＜50 | ＜50 | ＜50 |
| Cetane value | 30.9 | 30.6 | 30.1 |
| Cetane value improvement value | 10.3 | 10.0 | 10.8 |
| Boiling range ASTM D-86, ℃ | |||
| IBP | 205 | 197 | 195 |
| 10％ | 218 | 220 | 218 |
| 50％ | 248 | 255 | 260 |
| FBP | 370 | 368 | 372 |
Claims (9)
1. a method of being produced stop bracket gasoline by poor ignition quality fuel, diesel raw material oil-hydrogen mixture is first in the first reaction zone and Hydrobon catalyst contact reacts, the reaction effluent of the first reaction zone enters second reaction zone and hydrocracking catalyst contact reacts without separation, the reaction effluent of second reaction zone is through cooling, after separation, obtain hydrogen-rich gas and product liquid, it is characterized in that, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is more than 50%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, more than its mononuclear aromatics content is increased to 40 quality %,
When diesel raw material oil nitrogen content is 700 μ g/g-2000 μ g/g, Hydrobon catalyst is 5: 1～1: 1 with hydrocracking catalyst admission space ratio, when diesel raw material oil nitrogen content is less than 700 μ g/g, Hydrobon catalyst is 1: 1～1: 5 with hydrocracking catalyst admission space ratio.
2. in accordance with the method for claim 1, it is characterized in that, control the aromatic saturation degree of depth of the first reaction zone, with diesel raw material oil phase ratio, in the reaction effluent of the first described reaction zone, the saturation exponent of dicyclo and the above aromatic hydrocarbons of dicyclo is more than 60%, and the liquid ingredient of reaction effluent of the first reaction zone of take is benchmark, more than its mononuclear aromatics content is increased to 50 quality %.
3. in accordance with the method for claim 1, it is characterized in that, the boiling spread of described diesel raw material oil is 165～400 ℃, and total aromaticity content is higher than 65 quality %, and wherein the content of dicyclo and the above aromatic hydrocarbons of dicyclo is higher than 40 quality %.
4. in accordance with the method for claim 1, it is characterized in that, described diesel raw material grease separation catalytic cracking light cycle oil, heavy catalytic cycle oil, the straight-run diesel oil of naphthenic base crude, the diesel oil distillate of the coker gas oil of naphthenic base crude, coal direct liquefaction oil are, one or more in the diesel oil distillate of coal tar.
5. in accordance with the method for claim 1, it is characterized in that, the first described reaction zone and the reaction conditions of second reaction zone are: hydrogen dividing potential drop 3.0～10.0MPa, 300～450 ℃ of temperature of reaction, hydrogen to oil volume ratio 400～1600Nm
3/ m
3, volume space velocity 0.2～2.5h during liquid
-1.
6. in accordance with the method for claim 1, it is characterized in that, the first described reaction zone and the reaction conditions of second reaction zone are: hydrogen dividing potential drop 4.0～6.5MPa, 350～430 ℃ of temperature of reaction, hydrogen to oil volume ratio 500～1200Nm
3/ m
3, volume space velocity 0.4～1.5h during liquid
-1.
7. in accordance with the method for claim 1, it is characterized in that, when diesel raw material oil nitrogen content is 700 μ g/g-2000 μ g/g, Hydrobon catalyst is 3: 1～1: 1 with hydrocracking catalyst admission space ratio, when diesel raw material oil nitrogen content is less than 700 μ g/g, Hydrobon catalyst is 1: 1～1: 2 with hydrocracking catalyst admission space ratio.
8. in accordance with the method for claim 1, it is characterized in that, described Hydrobon catalyst is to load on composite alumina and/or combined oxidation silicon carrier Shang VIII family's base metal and/or group vib non-precious metal catalyst.
9. in accordance with the method for claim 1, it is characterized in that, described hydrocracking catalyst is to load on complex carrier Shang VIII family's base metal and/or group vib non-precious metal catalyst, in oxide compound and take catalyzer total amount as benchmark, catalyzer mesolite content is the heavy % of 1-90, the heavy % of aluminum oxide 5-80, the heavy % of metal component 3～30 of the heavy % of group VIII metal component 1～15, group vib.
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| CN102433156B (en) * | 2011-10-03 | 2016-03-16 | 何巨堂 | A kind of different boiling ranges height aromatic hydrocarbons high-density hydrocarbon oil hydrogenation transforms combined method |
| CN103184073B (en) * | 2011-12-31 | 2015-04-29 | 中国石油化工股份有限公司 | Hydrocracking method for producing gasoline blending component with high octane value |
| CN103214332B (en) * | 2012-01-18 | 2015-03-18 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbons and high-quality oil products from catalytically cracked diesel |
| CN103773469B (en) * | 2012-10-25 | 2016-08-24 | 中国石油化工股份有限公司 | A kind of method of hydrotreating being produced high-value product by catalytic cracking diesel oil |
| CN105273745B (en) * | 2014-05-29 | 2017-02-15 | 中国石油化工股份有限公司 | Low-grade diesel oil selective hydrogenation aromatic hydrocarbon removing method |
| CN106947528B (en) * | 2016-01-06 | 2019-03-19 | 中国石油化工股份有限公司 | A kind of hydrogenating conversion process containing aromatics diesel |
| CN106947529B (en) * | 2016-01-06 | 2019-03-19 | 中国石油化工股份有限公司 | A method of the conversion production gasoline of cut fraction hydrogenation containing aromatics diesel |
| CN107345154B (en) * | 2016-05-05 | 2019-04-12 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking of poor ignition quality fuel |
| CN108102703B (en) * | 2016-11-24 | 2020-06-09 | 中国石油化工股份有限公司 | Processing method of catalytic diesel 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 |
| CN112745920B (en) * | 2019-10-30 | 2022-06-28 | 中国石油化工股份有限公司 | Hydrocracking method for producing high-octane gasoline |
| CN115216337B (en) * | 2021-04-15 | 2023-10-10 | 中国石油化工股份有限公司 | Production method of high-octane gasoline |
| CN115703977B (en) * | 2021-08-10 | 2024-02-09 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbon and clean fuel oil |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1986747A (en) * | 2005-12-23 | 2007-06-27 | 中国石油化工股份有限公司 | Diesel oil fraction hydrogenating modification process |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1986747A (en) * | 2005-12-23 | 2007-06-27 | 中国石油化工股份有限公司 | Diesel oil fraction hydrogenating modification process |
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