CN1054150C - Catalyst for hydrocracking diesel oil - Google Patents
Catalyst for hydrocracking diesel oil Download PDFInfo
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- CN1054150C CN1054150C CN96109877A CN96109877A CN1054150C CN 1054150 C CN1054150 C CN 1054150C CN 96109877 A CN96109877 A CN 96109877A CN 96109877 A CN96109877 A CN 96109877A CN 1054150 C CN1054150 C CN 1054150C
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Abstract
The present invention relates to a hydrogenation converting catalyst for hydrocarbon oil. A carrier is composed of a molecular sieve, aluminum oxide and non-shaping silicone base substances. Hydrogenation metal constituents are tungsten and nickel, and an auxiliary agent can be added. The present invention is suitable for the hydrogenation conversion of petroleum distillation fraction with the temperature of 150 to 400DEGC, and is especially suitable for enhancing the cetane number of diesel oil with bad quality, reducing aromatic content and the hydrogenation converting process of desulphurization and denitrification. The present invention is adopted to hydrotreat the diesel oil with bad quality under the conditions of hydrogenation conversion and high space velocity (1.0 to 3h<-1>), the contents of S, N and aroylation industrial hydrocarbon are reduced, the cetane number of the product is enhanced by more than 10 units, and more than 95w% of diesel oil yield is obtained.
Description
The present invention relates to a kind of hydrocarbon oil hydrogenation conversion catalyst.Especially for the catalyzer that improves the diesel cetane-number technological process.
In petroleum refining industry, increase along with various secondary processing process treatment capacities, the particularly widespread use of catalytic cracking technology, the ratio that raw material is mixed residual oil or heavy oil constantly increases, produce a large amount of sulphur, nitrogen and aromaticity content height, cetane value is low, the catalytic cracking light cycle oil (LCO) of storage stability difference, be difficult to find the diesel component of competent high hexadecane value to be in harmonious proportion with it, cause the downgrade of diesel oil.Therefore, people are demanding developing novel method, the novel process that can improve the poor ignition quality fuel quality urgently.
And meanwhile environmental protection institution has proposed harsh more requirement to the diesel oil index, defines high sulfur content, aromaticity content and the minimum cetane number of diesel oil.The new spec about derv fuel oil of U.S. environment protection mechanism (EPA) promulgation comes into effect in October, 1993; comprising sulphur content＜500ppm; aromaticity content＜35 (v) %; the cetane value index is not less than 40, and stipulates the oxynitride (NO of the heavy gas oil engine of the U.S. in 1998
x) quantity discharged must be reduced to 20%, therefore is the environmental requirement of satisfying the nineties, the refinery must formulate far-reaching plan in conjunction with following product specification index, effectively improve diesel quality.
The source of diesel oil is very extensive, comprises straight-run diesel oil, coker gas oil and catalytic cracking diesel oil (LCO), is difficult to find a kind of single prioritization scheme.For straight-run diesel oil, light coker gas oil (LCGO), its cetane value is qualified substantially or approaching qualified.The main purpose of this class diesel oil hydrofining often is to solve S, N and stability problem.
For those diesel oil of from second-rate crude oil such as naphthenic base crude, producing or a large amount of low-cetane LCO, because the component that is contained mainly is a naphthalene class aromatic hydrocarbons, cetane value is very low, have only about 20, therefore, have only by deep hydrogenation is saturated and take off aromatic hydrocarbons or hydrocracking just might increase substantially diesel cetane-number.The deep hydrogenation saturation history of poor ignition quality fuel must adopt to contain noble metal catalyst and carry out under extremely harsh processing condition, therefore, is difficult to economically be accepted by people.And hydrocracking process certainly leads to part gasoline, certainly will make the diesel oil shortage situation that has existed at present more become to worsening.
It is hydrogenation component (WO that US 4820403 points out to adopt Ni-W
3Content is 15w%-20w%, and NiO content is 1.5w%-4.0w%), carrier is made up of ultra-steady Y molecular sieve (25w%-60w%) and aluminum oxide.When aromaticity content is higher in the light cycle oil (LCO), adopt this catalyzer single hop list agent processing boiling range, its hydrodenitrification, hydrogenating desulfurization and arene saturating activity are higher, and this catalyzer can improve the selectivity of petroleum naphtha, reduces C
1-C
5Gas products.This technology is that the yield of diesel oil is very low based on the production petroleum naphtha.
Adopt hydrotreating catalyst to handle diesel oil, general objects is that to carry out aromatic hydrocarbons saturated, improves oil product color and oxidation stability, produces low-sulfur diesel-oil, as WO 9417157, US 5068025, but little to the cetane value increase rate of poor ignition quality fuel.
The objective of the invention is to prepare the hydrogenation conversion catalyst that a kind of maximum is produced diesel oil, under the hydrocracking condition, make poor ignition quality fuel when removing impurity such as sulphur, nitrogen and aromatic hydrocarbons, naphthenic hydrocarbon open loop with aromatic hydrocarbons saturated back generation, generation has the high hexadecane value component of side chain, thereby increase substantially diesel cetane-number, and to avoid macromolecular cleavage be small molecules, guarantee high diesel yield.The present invention also aims in addition, simplify the treatment process of poor ignition quality fuel, reduce production costs and the catalyzer cost, and find the processing condition that are suitable for catalyzer of the present invention.
According to the reaction mechanism of aromatic saturation and ring opening, open loop and chain-breaking reaction take place at first at hydrogenation sites generation saturated reaction in aromatic hydrocarbons then on acid sites.According to this principle, the primary problem of the present invention is to guarantee that catalyzer has enough hydrogenation activities, needing earlier saturated precondition to satisfy open loop, secondly is to guarantee proper acidic center and strength of acid, with needs that adapt to ring-opening reaction and the generation that suppresses the chain rupture cracking reaction.
Catalyzer of the present invention be a kind of be carrier with molecular sieve, aluminum oxide, amorphous Si-Al, support hydrogenation metal and make.The used hydrogenation active metals of catalyzer is W, Ni.Can add auxiliary agent in the catalyzer, auxiliary agent can be a fluorine.
It is WO that catalyzer of the present invention is formed (is benchmark with the catalyzer)
310w%-30w%, NiO 2w%-15w%, molecular sieve 5w%-45w%, aluminum oxide 30-70w%, amorphous silicon aluminium 5w%-25w%.Its best group becomes WO
315w%-25w%, NiO 4w%-10w%, molecular sieve 10w%-35w%, aluminum oxide 40w%-60w%, amorphous aluminum silicide 8w%-20w%, auxiliary agent 1w%-9w%.
Preparation of catalysts method of the present invention is:
(1) with molecular sieve and macroporous aluminium oxide and amorphous aluminum silicide dry powder mixing, add extrusion aid (as the sesbania powder) and bonding agent (a kind of crystalline phase is that the little porous aluminum oxide and the nitric acid peptization of pseudo-boehmite forms), be mixed into paste, extrusion, descended dry 2-6 hour at 100-120 ℃, 400-600 ℃ roasting 2-6 hour, make carrier.The molecular sieve that is applicable to catalyzer of the present invention can be a Y zeolite.
(2) adopt the carrier of tungsten, nickel steeping fluid dipping (1) gained, 100-120 ℃ dry 2-6 hour down, 400-600 ℃ roasting 2-6 hour, make catalyzer.
(3) also available a kind of solution impregnation catalyst (2) that contains auxiliary agent, 100-120 ℃ dry 2-6 hour down, 400-600 ℃ roasting 2-6 hour, make catalyzer.
In the catalyst preparation process of the present invention, the carrier that can also obtain with the citric acid solution preimpregnation (1) of 2%-10%, this carrier carries out step (2) after filtering again.
Described molecular sieve is the Y zeolite of handling through high-temperature water vapor, and after handling through the high-temperature water vapor of certain hour, the aluminium atom is deviate from lattice after the hydrolysis of Al-O key, acid sites is reduced, the acidity of molecular sieve changes, and lattice constant dwindles simultaneously, and the stability of molecular sieve strengthens.The total acid of molecular sieve is controlled at 0.5-1.1mmol/g (meleic acid), and lattice constant is controlled at 2.436-2.444nm.The temperature of steam-treated is that 400-650 ℃, pressure are 0.05-0.2MPa, and the treatment time is 1-4 hour.
Described molecular sieve raw material be a kind of be method by Chinese patent 90102645.X record.Be NH
4The low sodium Y zeolite of high silicon that the NaY molecular sieve is handled with the hexafluorosilicic acid aqueous ammonium, its lattice constant is generally 2.449-2.453nm, degree of crystallinity＞95%, SiO
2/ Al
2O
3Mol ratio 5-40.This molecular sieve has is handling the characteristics that the post crystallization degree does not descend and guarantees higher specific surface area through high-temperature water vapor.Therefore, be particularly suitable for main acidic components as catalyzer of the present invention.
Used aluminum oxide, pore volume are 0.8-1.1ml/g, surface-area 230-400m
2/ g, used crystalline phase is that the pore volume of the little porous aluminum oxide of pseudo-boehmite is 0.4-0.6ml/g, surface-area 180-340m
2/ g, alumina trihydrate content＜3w%.The SiO of used amorphous silicon aluminium
2Content 10w%-90w%, pore volume 0.56-1.08ml/g, specific surface area 220-360m
2/ g.
Catalyzer of the present invention used tungsten salt in preparation process is generally metatungstic acid amine, ethyl ammonium metawolframate, and used nickel salt is nickelous nitrate or nickelous carbonate.
The metal loading mode also can adopt the mixed mode of pinching to add.
Also available citric acid carries out preimpregnation before this external supported carrier metal, improves activity of such catalysts.
Adopt catalyzer of the present invention, under the hydrocracking condition, handle poor ignition quality fuel, at temperature of reaction 34 0-390 ℃, pressure 4.0-8.0MPa, liquid air speed (V) 1-3h
-1, under the processing condition of hydrogen/oil ratio 500-1500 (V), diesel-fuel cetane number improves ten more than the unit, and diesel yield＞95w%, and this catalyzer is that a kind of to produce diesel oil with maximum be the effective catalyst of the poor ignition quality fuel hydrocracking of purpose.
The poor ignition quality fuel of this catalyst treatment can be catalytic cracking LCO, also can be the mixing oil of LCO and other straight-run diesel oil or coker gas oil, or other low-cetane poor ignition quality fuel.
Compared with prior art because the molecular sieve that catalyzer of the present invention adopts has good open-loop performance, and the amorphous aluminum silicide and the alumina host that are mixed with proper ratio are carrier, good Ni, W is the hydrogenation metal component to select the saturated performance of hydrogenation for use, make the saturated performance of hydrogenation and the selective opening performance of catalyzer reach best coupling, thereby make catalyzer both have saturated performance of good hydrogenation and open loop activity, can effectively suppress cracking reaction again, reach the purpose that increases substantially cetane value, guarantees diesel yield.
Further describe characteristics of the present invention below by example.
Example .1
(silica alumina ratio is 10.01, and lattice constant is 2.440nm, Na by patent CN90102654.X method synthetic high-silicon Y-Zeolite SSY in employing
2O content is 0.05w%, and relative crystallinity is 99%) be 650 ℃ in temperature, under the pressure of pressure 0.1MPa, hydrothermal treatment consists 1 hour, its degree of crystallinity are 97%, and lattice constant 2.305nm, total acid are 0.61mmol/g, and this molecular sieve is F-1
Comparative example .1
Get Wenzhou NH4Y molecular sieve (relative crystallinity is 95.9%, and lattice constant is 2.464nm, and silica alumina ratio is 9) 1000 grams, exchange 1 hour (sieve/liquor ratio is 1/10) with the 2M aqueous ammonium nitrate solution down at 90 ℃, filter, use deionized water wash, 110 ℃ of dryings 2 hours, 600 ℃, hydrothermal treatment consists is 2 hours under the 0.2MPa, the preparation ultra-steady Y molecular sieve, its degree of crystallinity is 72%, lattice constant 2.432nm, total acid are 0.51mmol/g, and this overtemperature molecular sieve is F-2.
Example .2
Get F-1 molecular sieve 200,100 grams, add 75 gram amorphous silicon aluminiums and 500 gram aluminum oxide respectively, adding 115 gram crystalline phases again is aluminum oxide (pore volume 0.50ml/g, the specific surface area 210m of pseudo-boehmite
2/ g) become bonding agent with 190ml0.2M nitric acid peptization, mixed rolling, extrusion, 120 ℃ of dryings 2 hours, 550 ℃ of roastings 4 hours, carrier is S-1, S-2.
Comparative example .2
Add 300 gram aluminum oxide with F-2100 gram, add example 2 described tackiness agents 200 grams again, mixed rolling, extrusion, 110 ℃ of dryings 4 hours, 550 ℃ of roastings 4 hours, carrier is S-3.
Example .3
Getting S-1100 gram is 8% citric acid solution dipping 2 hours with 200ml concentration, filters, and filters bar and (contains WO with tungsten, the nickel steeping fluid of 200ml
356%, NiO 18%) dipping 2 hours, filter, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 5 hours, catalyzer is C-1.
Example 4
Adopt each 100 gram of S-1, S-2, (contain WO with 180ml nickel, tungsten steeping fluid
350w%, NiO 22w%) dipping is 2 hours, filter, and 100 ℃ of dryings 4 hours, 500 ℃ of roastings 5 hours, catalyzer is C-2, C-3
Comparative example 3
Get the S-3100 gram, the tungsten, the nickel steeping fluid that add 200ml (contain WO
360w%, NiO 16w%) dipping is 2 hours, filter, and 110 ℃ of dryings 4 hours, 500 ℃ of roastings 4 hours, catalyzer is C-4.
Example 5
Get the ammonium fluoride solution that C-1150 gram adds 300ml4w% and under room temperature, stirred 1 hour, 110 ℃ of dryings 4 hours, 500 ℃ of roastings 4 hours.Catalyzer is C-5.
Comparative example 4
Get S-1100 gram,, filter with Mo, Ni steeping fluid dipping 2 hours, 110 ℃ of dryings 2 hours, 500 ℃ of roastings 4 hours, catalyzer is C-6.
Comparative example .5
C-7 is industrial application Hydrobon catalyst FH-5, and C-8 is for pressing the catalyzer of US4820403 preparation.The composition of C-1～C-8 sees Table 1.
The composition of table .1 catalyzer
| Catalyzer | Metal component, w% | Molecular sieve, w% | Carrier | Auxiliary agent |
| C-1 | WO 3(22.1）NiO(7.2) | 23 | Amorphous silicon aluminium+Al 2O 3+SSY | |
| C-2 | WO 3(19.2)NiO(6.8) | 23 | Amorphous silicon aluminium+Al 2O 3+SSY | |
| C-3 | WO 3(19.2)NiO(6.8) | 13 | Amorphous silicon aluminium+Al 2O 3+SSY | |
| C-4 | WO 3(19.2)NiO(6.4) | 20 | Al 2O 3+USY | |
| C-5 | WO 3(17.9)NiO(7.4) | 23 | Amorphous silicon aluminium+Al2O3+SSY | F(4.0) |
| C-6 | MoO 3(16.1)NiO(8.1) | 23 | Amorphous silicon aluminium+Al 2O 3+SSY | |
| C-7 | WO 3.MoO 3.NiO | 0 | Siliceous Al 2O 3 | |
| C-8 | WO 3(18.0)NiO(2.0) | 35 | Al 2O 3+ molecular sieve |
Example .6
This example is raw material with toluene, under identical reaction conditions, catalyzer C-1～C-8 is carried out the contrast experiment of hydrocracking, and reaction conditions sees Table 2, and reaction result sees Table 3.
The appreciation condition of table 2. catalyzer
| Pressure MPa | Air speed (LHSV) h -1 | Temperature of reaction ℃ | Hydrogen/hydrocarbon volume ratio |
| 6.0 | 2.0 | 380 | 1500 |
The micro anti-evaluation result of table 3. catalyzer
| Catalyzer | Toluene open loop rate w% | Toluene conversion w% |
| C-1 | 21 | 42 |
| C-2 | 15 | 36 |
| C-3 | 14 | 38 |
| C-4 | 19 | 33 |
| C-5 | 42 | 62 |
| C-6 | 16 | 31 |
| C-7 | 10 | 36 |
| C-8 | 43 | 59 |
Catalyzer is through the organic acid prognosis as can be seen by table .3, and its toluene open loop activity and toluene conversion have raising slightly, and the amplitude that improves after the fluoridize modification is bigger.C-6 compares with C-2, though the toluene open loop is high slightly, toluene conversion is low, illustrates that adopting W, Ni is metal component, and it is the catalyzer of metal component that its toluene conversion will be higher than with Mo, Ni.Result by C-4 finds out, adopts the USY molecular sieve catalyst, and its open-loop performance is better than C-2, but its toluene conversion is lower.The evaluation result of C-7 shows that toluene open loop activity and toluene conversion are all lower, and the open loop activity of C-8 is the highest, and toluene conversion and C-5 are close.
Example .7
This example is on 200ml small test device, and adopting the higher poor ignition quality fuel of a kind of aromaticity content is raw material, and catalyzer C-1, C-5 are estimated, and the results are shown in table .4.
The small-sized evaluation result of table 4.
| Catalyzer | C-1 | C-5 | |
| Appreciation condition: | |||
| Temperature (℃) | 370 | 370 | |
| Pressure (MPa) | 6.0 | 6.0 | |
| Hydrogen/oil ratio (V) | 500 | 500 | |
| Air speed (Vh -1) | 1.0 | 1.0 | |
| Feedstock property | Product property | ||
| Density (20 ℃), g/cm 3 | 0.8955 | 0.8695 | 0.8649 |
| IBP/10％ | 199/241 | 126/215 | 119/209 |
| 30％/50％ | 254/369 | 235/256 | 231/250 |
| 70％/90％ | 285/310 | 270/300 | 271/301 |
| 95％/EBP | 317/330 | 311/327 | 311/329 |
| Cetane value | 26 | 40.9 | 41.8 |
| Diesel yield, V% | - | ＞95 | ＞95 |
As can be seen from Table 4, adopt the higher poor ignition quality fuel of catalyst treatment aromaticity content of the present invention, its cetane value can improve 14 units, diesel yield＞95 V%, promptly this invention catalyzer can guarantee on the little basis of diesel yield loss poor ignition quality fuel to be handled the raising cetane value.
Example .8
It is raw material that this example adopts a kind of light cycle oil (180-350), estimates comparative catalyst C-7, C-8 and catalyzer C-5 of the present invention, the evaluating data .5 that sees the following form.
The evaluation result of table 5.C-7, C-8 and C-5
| Catalyzer | C-7 | C-8 | C-5 | |
| Reaction conditions: | ||||
| Pressure (MPa) | 6.0 | 6.0 | 6.0 | |
| Hydrogen/oil ratio (V) | 1000 | 800 | 800 | |
| Air speed (LHSV h -1) | 1.0 | 1.5 | 1.5 | |
| Temperature of reaction (℃) | 360 | 360 | 360 | |
| Feedstock property | Product property | |||
| Density (20 ℃), g/cm 3 | 0.8833 | 0.8753 | 0.8600 | 0.8650 |
| Boiling range, (℃) | ||||
| 10％ | 239 | 221 | 169 | 200 |
| 30％ | 259 | 258 | 220 | 248 |
| 50％ | 278 | 276 | 269 | 271 |
| 70％ | 309 | 304 | 288 | 286 |
| 90％ | 331 | 328 | 324 | 326 |
| Diesel yield, V% | 98.5 | 89.3 | 95.8 | |
| Cetane value | 32.0 | 37.0 | 40.0 | 43.5 |
Adopt catalyzer of the present invention, cetane value can improve 11.5 units, diesel yield＞95V%.Adopt Hydrobon catalyst C-7, at air speed 1.0 (h
-1), under the reaction conditions that temperature is 360 ℃, cetane value only improves 5 units.Adopt hydrocracking catalyst C-8, cetane value improves 8 units, and diesel yield is lower, illustrates that this catalyzer compares with catalyzer of the present invention, and the driffractive ring selectivity is relatively poor, and the chain rupture selectivity is better, has therefore reduced the yield of diesel oil.This shows that catalyzer of the present invention adding under the conversion system condition, is superior to hydrofining and hydrocracking catalyst to the diesel oil hydroprocessing effect.
Example .9
For understanding catalyzer of the present invention to the conversion capability of poor ignition quality fuel (hydrogenation is saturated, hydrodenitrification and hydrogenating desulfurization), on small-sized evaluating apparatus, adopt single hop list agent (catalyzer is C-5) once to pass through flow process, with poor ignition quality fuel (high nitrogen, high-sulfur, high aromaticity content) is raw material, carry out hydrocracking, processing condition are: the hydrogen dividing potential drop is 6.0MPa, hydrogen to oil volume ratio 1000, liquid air speed 2.0h
-1
Evaluation result is as table .6
Table .6
| Feedstock property | Product property | |
| Density (20 ℃) g/cm 3 | 0.9123 | 0.8705 |
| Sulphur μ g/g | 3564 | 120 |
| Nitrogen μ g/g | 850 | 7.0 |
| Cetane value | 30.0 | 41.0 |
| Boiling range (ASTMD86) ℃ | ||
| 10％ | 245 | 235 |
| 30％ | 263 | 252 |
| 50％ | 283 | 276 |
| 70％ | 311 | 307 |
| 90％ | 353 | 365 |
| ＜180 ℃ of cut V% | Do not have | 3.3 |
.6 finds out by table, adopt catalyzer of the present invention to transform poor ignition quality fuel, its sulphur, nitrogen content have reduction significantly, cetane value improves 11 units, promptly this catalyst treatment poor ignition quality fuel has preferably the active and hydrogenating desulfurization of aromatic saturation and ring opening, hydrodenitrification ability, is a kind of effective inferior diesel hydrogenation catalyst.
Claims (8)
1, a kind of poor ignition quality fuel hydrogenation conversion catalyst, the carrier by aluminum oxide, amorphous aluminum silicide and molecular sieve are made supports hydrogenation active metals, it is characterized in that the WO that consists of of catalyzer
310-30w%, NiO2-15w%, molecular sieve 5-45w%, aluminum oxide 30-70w%, amorphous aluminum silicide 5-25w%, wherein molecular sieve is a Y zeolite, and its infrared total acid is 0.5-1.1mmol/g, and lattice constant is 2.436-2.444nm.
2,, it is characterized in that the WO that consists of of catalyzer according to the catalyzer of claim 1
315-25w%, NiO4-10w%, molecular sieve 10-35w%, aluminum oxide 40-60w%, amorphous aluminum silicide 8-20w%, fluorine 1-9W%.
3, a kind of claim 1 Preparation of catalysts method:
(1) with molecular sieve and aluminum oxide and amorphous aluminum silicide dry powder mixing, add extrusion aid and make paste, extrusion was descended dry 2-6 hour at 100-120 ℃, again at 400-600 ℃ of following roasting 2-6 hour, obtained carrier;
(2) carrier that obtains with tungstenic, nickel steeping fluid dipping (1) descended dry 2-6 hour at 100-120 ℃, again at 400-600 ℃ of following roasting 2-6 hour, obtained catalyzer.
4,, it is characterized in that said molecular sieve component is by lattice constant 2.449-2.453nm, degree of crystallinity＞95%, SiO according to the method for claim 3
2/ Al
2O
3The Y zeolite of mol ratio 5-40 obtained under 400-650 ℃ and 0.05-0.2MPa in hydrothermal treatment consists 1-4 hour.
5, according to the method for claim 3, it is characterized in that the catalyzer that obtains with fluorine-containing solution impregnation (2), and 100-120 ℃ dry 2-6 hour down, again at 400-600 ℃ of following roasting 2-6 hour.
6, according to the method for claim 3, it is characterized in that flooding the carrier that (1) obtains with the citric acid solution of 2-10%, carry out step (2) after the filtration.
7, a kind of purposes of claim 1 catalyzer is characterized in that this catalyzer is used for poor ignition quality fuel and transforms under the hydrocracking condition, particularly the hydrocracking of low cetane number diesel.
8,, it is characterized in that at 340-390 ℃, 4.0-8.0MPa, air speed 1-3h according to the purposes of claim 7
-1, under the condition of hydrogen/oil volume than 500-1500, catalyzer is contacted with the poor ignition quality fuel raw material.
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|---|---|---|---|
| CN96109877A CN1054150C (en) | 1996-09-27 | 1996-09-27 | Catalyst for hydrocracking diesel oil |
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|---|---|---|---|
| CN96109877A CN1054150C (en) | 1996-09-27 | 1996-09-27 | Catalyst for hydrocracking diesel oil |
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| CN1054150C true CN1054150C (en) | 2000-07-05 |
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| CN1102663A (en) * | 1993-08-30 | 1995-05-17 | 日本石油株式会社 | Process for hydrotreating heavy hydrocarbon oil |
-
1996
- 1996-09-27 CN CN96109877A patent/CN1054150C/en not_active Expired - Lifetime
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4820403A (en) * | 1987-11-23 | 1989-04-11 | Amoco Corporation | Hydrocracking process |
| CN1053635A (en) * | 1988-08-29 | 1991-08-07 | 美国环球油品公司 | Improve the selection method of hydrotreating of the color and the colour stability of hydrocarbon-fraction |
| US5068025A (en) * | 1990-06-27 | 1991-11-26 | Shell Oil Company | Aromatics saturation process for diesel boiling-range hydrocarbons |
| WO1994017157A1 (en) * | 1993-01-28 | 1994-08-04 | Union Oil Company Of California | Color removal with post-hydrotreating |
| CN1102663A (en) * | 1993-08-30 | 1995-05-17 | 日本石油株式会社 | Process for hydrotreating heavy hydrocarbon oil |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2463025A1 (en) | 2005-04-21 | 2012-06-13 | China Petroleum & Chemical Corporation | Ni/Mo/W supported hydrogenation catalyst containing P or F and process for hydrocarbon hydrogenation |
| CN100448952C (en) * | 2005-04-29 | 2009-01-07 | 中国石油化工股份有限公司 | Hydrogenation cracking catalyst composition containing zeolite |
| US8883669B2 (en) | 2005-04-29 | 2014-11-11 | China Petroleum & Chemical Corporation | Hydrocracking catalyst, a process for producing the same, and the use of the same |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1178238A (en) | 1998-04-08 |
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