CN104549556B - Method for improving selectivity of catalyst - Google Patents
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Abstract
The invention relates to a method for improving selectivity of a catalyst. A catalyst selectivity regulation and control process is increased between a desulfurization process and a normal production process, and the catalyst selectivity regulation and control process is that activity catalytic raw materials are in contact with the catalyst for 24-96h in an atmosphere of activity catalytic gas under activity catalytic reaction conditions, wherein the activity catalytic gas comprises hydrogen gas and hydrogen sulfide, and based on the whole activity catalytic gas, the volume fraction of the hydrogen gas is not less than 70%, and the volume fraction of hydrogen sulfide is 0.2%-5%; and the normal production process is that gasoline raw material is in contact with the catalyst in the atmosphere which is rich in the hydrogen gas under normal reaction conditions to be in hydrogenation reaction. By adopting the method provided by the invention, the selectivity of the catalyst can be improved. Compared with the prior art, under the situation that the sulfur content in a gasoline product is the same, the olefin saturation rate is lower and the loss in octane number of a product is smaller.
Description
Technical field
The present invention relates to a kind of method for improving catalyst choice.
Background technology
It is well known that air pollution is a serious environmental problem, and substantial amounts of engine emission is to cause air dirty
One of major reason of dye.In recent years, it is environmental protection, countries in the world propose tightened up limit to the composition of engine fuel
System, especially sulfur content.Require that sulfur content in gasoline is less than 50 μ g/g in the standard that Beijing and Shanghai City have been carried out.
The working ability of China's catalytic cracking accounts for the large percentage of secondary operations, and catalytically cracked gasoline is the master of merchantable gasoline
Originate, other gasoline components are few, mediation ability.Sulfur from gasoline pool in terms of various blend components, in catalytically cracked gasoline
It is the main source of sulfur in gasoline pool；Constantly rise especially as processing import sour crude amount, and catalyzed cracking processing
Continuous development of the raw material to heaviness direction, Sulfur Content in Catalytic Cracking Gasoline will be continuously maintained at higher level.Therefore drop
Low Sulfur Content in Catalytic Cracking Gasoline will become the main path of sulfur content in control motor petrol.
The sulfur content for reducing catalytically cracked gasoline can generally adopt catalytically cracked material weighted BMO spaces（Front-end hydrogenation）, catalysis
Cracking gasoline hydrodesulfurization（Back end hydrogenation）Or the connected applications of two ways.Wherein, catalytically cracked material pretreatment can be significantly
The sulfur content of catalytically cracked gasoline is reduced, but needs all to operate very under exacting terms in temperature and pressure, simultaneously as device
Treating capacity is big, causes hydrogen consumption also than larger, and these will all improve investment or the operating cost of device.Meanwhile, with catalytic cracking
The innovation of technology, the gradually application of catalytic cracking desulfurization auxiliary, the sulfur content of catalytic cracking gasoline of China's Some Enterprises can reach
To below 500 μ g/g.But if the sulfur content of catalytically cracked gasoline further will be reduced, be less than 50 μ g/g, then must be big
Amplitude improves the operating severity of catalytically cracked material hydrogenation plant, economically very uneconomical.
Therefore, compared with catalytically cracked material weighted BMO spaces technology, catalytic gasoline hydrogenation technology plant investment,
There is certain advantage in terms of production cost and hydrogen consumption.As catalytically cracked gasoline can be made using traditional hydrodesulfurizationprocess process
In have a large amount of saturations of high-octane olefin component and make loss of octane number very big, therefore, sinopec petrochemical industry science is ground
Study carefully institute and some other research and development institution develops the little RSDS of loss of octane number.But
It is how further to improve its selectivity, i.e., while deep desulfuration, further reduces product loss of octane number, be still
The problem for needing to solve.
WO2005037959 discloses a kind of raising selective hydrogenation desulfuration catalyst for catalytically cracking gasoline selectively side
Method.Catalytically cracked gasoline is first carried out absorption denitrogenation by the first step, obtains intermediate products；It is de- that intermediate products are carried out hydrogenation by second step
Sulphuring treatment.It is molten that denitrification adsorbent used is mainly exchanger resin, aluminium oxide, silicon dioxide, clay, organic or inorganic acid, polarity
Agent etc..
The content of the invention
The technical problem to be solved is how further to improve the selective problems of Hydrobon catalyst.
Method provided by the present invention is：Increase catalyst choice regulation and control between sulfidation and normal productive process
Process, described catalyst choice regulation process are to urge raw material living in the atmosphere for urging lively atmosphere body, in the case where reaction condition living is urged
24-96 hours are contacted with catalyst, it is described to urge lively atmosphere body to include hydrogen and hydrogen sulfide, on the basis of urging lively atmosphere body entirety, wherein
The volume fraction of hydrogen is not less than 70%, and the volume fraction of hydrogen sulfide is 0.2%-5%, and described normal productive process refers to gasoline
Raw material in the atmosphere of hydrogen-rich gas, contact with catalyst under normal reaction conditions and carry out hydrogenation reaction.
The one of which embodiment of the present invention, comprises the following steps：
（1）Fresh catalyst or regenerated catalyst are vulcanized,
（2）After sulfidation terminates, in adjustment response system, gas is to urge lively atmosphere body,
（3）Raw material living will be urged to introduce response system, and contact 32-90 hours in the case where reaction condition living is urged with catalyst,
（4）Normal reaction conditions are adjusted to, it is gasoline stocks that raw material living is urged in switching,
（5）In adjustment response system, gas is hydrogen-rich gas, and gasoline stocks are carried out with catalyst under normal reaction conditions
Reaction, in the hydrogen-rich gas, on the basis of hydrogen-rich gas entirety, the volume fraction of hydrogen is at least 70%, the volume of hydrogen sulfide
Fraction is less than 0.05%.
The boiling range of gasoline stocks of the present invention is 30-205 DEG C, and the volume fraction of alkene is 5%-60%, and sulfur content is
50-5000μg/g.Can be for catalytically cracked gasoline, catalytic cracking gasoline, coker gasoline, pressure gasoline, direct steaming gasoline wherein
The miscella of any one or several.Preferably catalytically cracked gasoline.
Catalytically cracked gasoline can be divided into n-alkane from composition（n-P）, isoparaffin（i-P）, cycloalkane（N）, alkene
Hydrocarbon（O）And aromatic hydrocarbons（A）Five components, the octane number of wherein n-alkane are low, and the longer octane number of carbochain is lower.Isoparaffin
Octane number is higher, and collateralization degree is higher, it is higher to arrange compacter octane number.Alkene, aromatic hydrocarbons are antiknock components, with virtue
The octane number of hydrocarbon is highest.China's catalytically cracked gasoline is presented high alkene, the feature of low arene content, and olefin(e) centent is generally 30
～50 volumes % or so, thus impact of the change of olefin(e) centent to catalytically cracked gasoline octane number is very big.Therefore, the present invention is carried
For method can further improve the selectivity of Hydrobon catalyst, i.e., while further deep desulfuration, reduce product
The loss of octane number.
Catalyst of the present invention be the vib metals on being supported on alumina support and/or silica-alumina supports and/or
Group VIII metallic catalyst, wherein vib metals are selected from molybdenum and/or tungsten, and group VIII metal is selected from cobalt and/or nickel.It is excellent
At least contain molybdenum and cobalt in the described catalyst of choosing, based on catalyst entirety, in terms of oxide, molybdenum and/or tungsten are 4-25
Weight %, cobalt and/or nickel 0.3-6 weight %.
Due to cobalt, nickel, molybdenum, tungsten oxide have hydrogenation activity, only with the presence of sulfide state just with compared with
High hydrogenation activity, accordingly, it would be desirable to the catalyst after fresh catalyst and regeneration is vulcanized so as to be converted into from oxidation state
Sulphided state.Described sulfidation can vulcanize for wet method or dry pre-sulfiding.The catalyst vulcanization speed and degree and sulfuration
Temperature has close relationship, and the state of cure (vulcanization) of catalyst has a ultimate value at each temperature, even if prolonging after reaching this value again
For a long time, the sulfur content on catalyst also substantially will not increase.The sulfidation terminates to refer to catalyst in reactor bed
After temperature reaches predetermined curing temperature, in reactor, in gas, the volume fraction of hydrogen sulfide is more than 1%, and no longer reduces.
The catalyst after sulfuration, exist desulphurizing activated center and two kinds of olefins hydrogenation active center it is active in
The heart.Therefore, the present inventor is had found by lot of experiments, increases and urge between sulfidation and normal productive process
Agent selective regulation process, can substantially shield one of which active center, so as to improve selectivity of catalyst.Described
Catalyst choice regulation process is will to urge raw material living in the atmosphere for urging lively atmosphere body, connect with catalyst under reaction condition living urging
Touch.The process can effectively cause coking charcoal to be covered in catalyst olefins hydrogenation active center, make catalyst hydrogenation of olefins
Saturated activity is substantially reduced, and desulphurizing activated center is valid protected, and the desulphurizing activated of catalyst is not lost substantially or is damaged
Lose very little.
It is described to urge lively atmosphere body to include hydrogen and hydrogen sulfide, on the basis of urging lively atmosphere body entirety, the volume of hydrogen preferably wherein
Fraction is not less than 80%, and the volume fraction of hydrogen sulfide is 0.3%-2%.
The boiling range for urging raw material living of the present invention is 30-350 DEG C, and wherein, the volume fraction of alkene is 5%-60%.
It is preferred that it is described urge raw material living in also contain aromatic hydrocarbons, wherein, the volume fraction of aromatic hydrocarbons is 5%-60%.
Described reaction condition living of urging is：In hydrogen dividing potential drop 0.6-2.0MPa, reaction temperature 200-350 DEG C, volume space velocity 1-
10h-1, hydrogen to oil volume ratio 50-400Nm3/m3, urge the response time living to be 48-88 hours.
After catalyst choice regulation process terminates, normal reaction conditions are adjusted to, and switching urges raw material living for gasoline original
Material, in adjustment response system, gas is hydrogen-rich gas, in the hydrogen-rich gas, on the basis of hydrogen-rich gas entirety, preferred hydrogen
Volume fraction be at least 85%, the volume fraction of hydrogen sulfide is less than 0.02%.Gasoline stocks under normal reaction conditions with catalysis
Agent is reacted, and reactor effluent enters high-pressure separator, isolates gas phase and liquid product, and gas phase is after depriving hydrogen sulphide
Recycle, liquid phase stream enters stripper, and stripping tower bottom effluent enters products pot as product.
Described normal reaction conditions are in 1.0～4.0MPa of hydrogen dividing potential drop, 200～460 DEG C of reaction temperature, volume space velocity 2
～8h-1, 200～1000Nm of hydrogen to oil volume ratio3/m3。
It is preferred that, the described reaction temperature for urging reaction living is higher than the reaction temperature of normal reaction 30～100 DEG C.Described urges
Volume space velocity 2～the 4h lower than the volume space velocity of normal reaction of reaction living-1。
The method provided using the present invention, can make in the case where catalyst desulfurizing activity is not lost substantially, and alkene adds
Hydrogen saturated activity declines to a great extent, and improves selectivity of catalyst.Compared with prior art, in gasoline products sulfur content identical
In the case of, alkene saturation factor is lower, and product loss of octane number is less.Also, the processing method of the present invention is simple, industrially holds
Easily implement.
Specific embodiment
The following examples will be further described to this method, but and be not so limited this method.With selectivity
The factor weighs selectivity of catalyst.
Selectivity factor adopts following definition：S=log（Sp/Sf）/log（Op/Of）.
In formula：S selectivity factors；SpGasoline products sulfur content；SfGasoline stocks sulfur content；OpGasoline products
Alkene mass content；OfGasoline stocks alkene mass content.
Used in comparative example and embodiment, the trade names of catalyst A, B are RSDS-21, RSDS-22, these catalyst
Produced by Sinopec catalyst Chang Ling branch company.
Comparative example 1
Using fresh A catalyst, A catalyst in reactor is vulcanized, after sulfuration terminates, by a kind of gasoline stocks D
（Its raw material oil nature is shown in Table 1）Contact with the A catalyst after sulfuration with hydrogen-rich gas and carry out under normal reaction conditions anti-
Answer, its reaction condition and gasoline products property are as shown in table 2.
From table 2 it can be seen that gasoline products desulfurization degree be 94.5 heavy %, alkene saturation factor be 27.3 volumes %, catalyst
Selectivity factor is 9.11.
Comparative example 2
Using two kinds of catalyst grading loadings of fresh A, B catalyst, A, B catalyst admission space ratio in the reactor
For A:B=85:15.A, B catalyst in reactor is vulcanized, after sulfuration terminates, by a kind of gasoline stocks E（Its raw material oiliness
Matter is shown in Table 1）Contact with A, B catalyst after sulfuration with hydrogen-rich gas and reacted under normal reaction conditions, its reaction
Condition and gasoline products property are as shown in table 2.
From table 2 it can be seen that gasoline products desulfurization degree be 98.3 heavy %, alkene saturation factor be 44.3 volumes %, catalyst
Selectivity factor is 6.99.
Embodiment 1
Using fresh A, B catalyst, A, B catalyst admission space ratio in the reactor is A:B=85:15.To reaction
In device, A, B catalyst is vulcanized, and after sulfuration terminates, in adjustment response system, gas is to urge lively atmosphere body, in urging lively atmosphere body, hydrogen
Volume fraction be 80%, H2The volume fraction of S is 1.5%, raw material living will be urged to introduce response system, and urging condition living for hydrogen point
Pressure 1.6MPa；Hydrogen-oil ratio 100Nm3/m3；Volume space velocity 4.0h-1；48h is contacted with catalyst under conditions of 360 DEG C of reaction temperature
Afterwards.The boiling range for urging raw material living is 30-350 DEG C, and wherein, the volume fraction of alkene is 30%.
Then normal reaction conditions are adjusted to, it is gasoline stocks that raw material living is urged in switching, and gas switches to hydrogen-rich in reactor
Gas, on the basis of hydrogen-rich gas entirety, the volume fraction of hydrogen is 82%, and the volume fraction of hydrogen sulfide is 0.01%.Gasoline is former
Material C and hydrogen-rich gas are contacted with A, B catalyst after process and are reacted under normal reaction conditions, its reaction condition and gasoline
Product property is as shown in table 3.
From table 3 it can be seen that product desulfurization degree be 94.6 heavy %, alkene saturation factor be 27.0 volumes %, catalyst choice
Sex factor is 9.27.
Embodiment 2
Using fresh A catalyst, A catalyst in reactor is vulcanized, after sulfuration terminates, gas in adjustment response system
For urging lively atmosphere body, in urging lively atmosphere body, the volume fraction of hydrogen is 82%, H to body2The volume fraction of S is 1.0%, and raw material living will be urged to draw
Enter response system, and urge condition hydrogen dividing potential drop 1.6MPa living；Hydrogen-oil ratio 200Nm3/m3；Volume space velocity 4.0h-1；Reaction temperature 350
48h is contacted with catalyst under conditions of DEG C, the boiling range for urging raw material living is 30-350 DEG C, wherein, the volume fraction of alkene is 25%,
The volume fraction of aromatic hydrocarbons is 30%.
Normal reaction conditions are adjusted to, it is gasoline stocks that raw material living is urged in switching, and gas switches to hydrogen-rich gas in reactor,
On the basis of hydrogen-rich gas entirety, the volume fraction of hydrogen is 85%, and the volume fraction of hydrogen sulfide is 0.01%, then allows gasoline former
Material D and hydrogen-rich gas are contacted with the A catalyst after process and are reacted under normal reaction conditions, and its reaction condition and gasoline are produced
Moral character matter is as shown in table 3.
From table 3 it can be seen that gasoline products desulfurization degree be 94.5 heavy %, alkene saturation factor be 27.3 volumes %, catalyst
Selectivity factor is 10.60.Compared with comparative example 1, the selectivity of the present embodiment is greatly improved.
Embodiment 3
Using fresh A, B catalyst, A, B catalyst admission space ratio in the reactor is A:B=85:15.To reaction
In device, A, B catalyst is vulcanized, and after sulfuration terminates, in adjustment response system, gas is to urge lively atmosphere body, in urging lively atmosphere body, hydrogen
Volume fraction be 85%, H2The volume fraction of S is 2.0%, raw material living will be urged to introduce response system, and urging condition hydrogen dividing potential drop living
1.6MPa；Hydrogen-oil ratio 100Nm3/m3；Volume space velocity 4.0h-1；72h is contacted with catalyst under conditions of 350 DEG C of reaction temperature, is urged
The boiling range of raw material living is 30-350 DEG C, and wherein, the volume fraction of alkene is 45%, and the volume fraction of aromatic hydrocarbons is 25%.
Normal reaction conditions are adjusted to, it is gasoline stocks that raw material living is urged in switching, and gas switches to hydrogen-rich gas in reactor,
On the basis of hydrogen-rich gas entirety, the volume fraction of hydrogen is 88%, and the volume fraction of hydrogen sulfide is 0.015%, then allows gasoline
Raw material D and hydrogen-rich gas are contacted with A, B catalyst after process and are reacted under normal reaction conditions, its reaction condition and vapour
Oil product property is as shown in table 3.
From table 3 it can be seen that gasoline products desulfurization degree be 98.2 heavy %, alkene saturation factor be 35.0 volumes %, catalyst
Selectivity factor is 9.28.Compared with comparative example 2, the selectivity of the present embodiment is greatly improved.
Table 1
| Material name | C | D | E |
| Density (20 DEG C), g/cm3 | 0.7740 | 0.7688 | 0.7923 |
| Sulfur, μ g/g | 1300 | 1000 | 3000 |
| Olefin(e) centent, volume % | 37.0 | 25.3 | 30.0 |
| Boiling range (ASTM D-86), DEG C | |||
| Initial boiling point | 78 | 75 | 77 |
| 10% | 94 | 90 | 98 |
| 50% | 126 | 115 | 132 |
| The end point of distillation | 205 | 194 | 198 |
Table 2
| Comparative example 1 | Comparative example 2 | |
| Raw oil | C | D |
| Catalyst | A+B | A |
| Reaction condition | ||
| Reaction temperature, DEG C | 303 | 292 |
| Hydrogen dividing potential drop, MPa | 1.6 | 1.6 |
| Hydrogen to oil volume ratio, Nm3/m3 | 400 | 400 |
| Volume space velocity, h-1 | 4.0 | 4.0 |
| Product property | ||
| S, μ g/g | 66 | 55 |
| Olefin(e) centent, volume % | 25.4 | 18.4 |
| Desulfurization degree, weight % | 94.9 | 94.5 |
| Alkene saturation factor, volume % | 31.4 | 27.3 |
| Selectivity factor | 7.92 | 9.11 |
Table 3
| Embodiment 1 | Embodiment 2 | Embodiment 3 | |
| Raw oil | C | D | E |
| Reaction condition | |||
| Catalyst | A+B | A | A+B |
| Reaction temperature, DEG C | 305 | 296 | 310 |
| Hydrogen dividing potential drop, MPa | 1.6 | 1.6 | 1.6 |
| Hydrogen to oil volume ratio, Nm3/m3 | 400 | 400 | 500 |
| Volume space velocity, h-1 | 4.0 | 4.0 | 4.0 |
| Product property | |||
| S, μ g/g | 70 | 48 | 55 |
| Olefin(e) centent, volume % | 27.0 | 19.0 | 19.5 |
| Desulfurization degree, weight % | 94.6 | 95.2 | 98.2 |
| Alkene saturation factor, volume % | 27.0 | 24.9 | 35.0 |
| Selectivity factor | 9.27 | 10.60 | 9.28 |
Claims (14)
1. it is a kind of improve catalyst choice method, it is characterised in that between sulfidation and normal productive process increase
Catalyst choice regulation process, described catalyst choice regulation process be urge raw material living in the atmosphere for urging lively atmosphere body,
24-96 hours are contacted in the case where reaction condition living is urged with catalyst, it is described to urge lively atmosphere body to include hydrogen and hydrogen sulfide, to urge lively atmosphere body
On the basis of entirety, wherein the volume fraction of hydrogen is not less than 70%, and the volume fraction of hydrogen sulfide is 0.2%-5%, it is described just
Often production process refer to gasoline stocks in the atmosphere of hydrogen-rich gas, contact with catalyst under normal reaction conditions and be hydrogenated with
Reaction, the boiling range for urging raw material living are 30-350 DEG C, and wherein, the volume fraction of alkene is 5%-60%.
2. in accordance with the method for claim 1, it is characterised in that comprise the following steps：
(1) fresh catalyst or regenerated catalyst are vulcanized,
(2), after sulfidation terminates, in adjustment response system, gas is to urge lively atmosphere body,
(3) raw material living will be urged to introduce response system, and will contact 32-90 hours in the case where reaction condition living is urged with catalyst,
(4) normal reaction conditions are adjusted to, it is gasoline stocks that raw material living is urged in switching,
(5) in adjusting response system, gas is hydrogen-rich gas, and gasoline stocks are reacted with catalyst under normal reaction conditions,
In the hydrogen-rich gas, on the basis of hydrogen-rich gas entirety, the volume fraction of hydrogen is at least 70%, the volume fraction of hydrogen sulfide
Less than 0.05%.
3. according to the method described in claim 1 or 2, it is characterised in that described sulfuration is that wet method vulcanizes or dry pre-sulfiding.
4. according to the method described in claim 1 or 2, it is characterised in that the sulfidation terminates to refer to catalysis in reactor
After agent bed temperature reaches predetermined curing temperature, in reactor, in gas, hydrogen sulfide volume fraction is more than 1%, and no longer reduces.
5. according to the method described in claim 1 or 2, it is characterised in that urge lively atmosphere body to include hydrogen and hydrogen sulfide, to urge lively atmosphere
On the basis of body entirety, wherein the volume fraction of hydrogen is not less than 80%, and the volume fraction of hydrogen sulfide is 0.3%-2%.
6. in accordance with the method for claim 1, it is characterised in that contain aromatic hydrocarbons in urging raw material living, wherein, the volume integral of aromatic hydrocarbons
Number is 5%-60%.
7. according to the method described in claim 1 or 2, it is characterised in that described reaction condition living of urging is：In hydrogen dividing potential drop 0.6-
2.0MPa, reaction temperature 200-350 DEG C, volume space velocity 1-10h-1, hydrogen to oil volume ratio 50-400Nm3/m3, urge the response time living to be
48-88 hours.
8. according to the method described in claim 1 or 2, it is characterised in that described normal reaction conditions be hydrogen dividing potential drop 1.0～
4.0MPa, 200～460 DEG C of reaction temperature, 2～8h of volume space velocity-1, 200～1000Nm of hydrogen to oil volume ratio3/m3。
9. according to the method described in claim 1 or 2, it is characterised in that the described reaction temperature for urging reaction living is more anti-than normal
The reaction temperature answered is high 30～100 DEG C.
10. according to the method described in claim 1 or 2, it is characterised in that the described volume space velocity for urging reaction living is more anti-than normal
Low 2～the 4h of volume space velocity for answering-1。
11. according to the method described in claim 1 or 2, it is characterised in that in the hydrogen-rich gas, with hydrogen-rich gas generally
Benchmark, the volume fraction of hydrogen are at least 85%, and the volume fraction of hydrogen sulfide is less than 0.02%.
12. according to the method described in claim 1 or 2, it is characterised in that the boiling range of described gasoline stocks is 30-205 DEG C,
The volume fraction of alkene is 5%-60%, and sulfur content is 50-5000 μ g/g.
13. according to the method described in claim 1 or 2, it is characterised in that described catalyst is to be supported on alumina support
And/or the vib metals in silica-alumina supports and/or group VIII metallic catalyst, wherein vib metals selected from molybdenum and/
Or tungsten, group VIII metal is selected from cobalt and/or nickel.
14. in accordance with the method for claim 13, it is characterised in that at least contains molybdenum and cobalt in described catalyst, to urge
Based on agent entirety, in terms of oxide, molybdenum and/or tungsten are 4-25 weight %, cobalt and/or nickel 0.3-6 weight %.
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| CN107043638B (en) * | 2016-02-05 | 2019-05-21 | 中国石油化工股份有限公司 | A method of improving catalyst for selectively hydrodesulfurizing selectivity |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5906730A (en) * | 1995-07-26 | 1999-05-25 | Mitsubishi Oil Co., Ltd. | Process for desulfurizing catalytically cracked gasoline |
| CN101116816A (en) * | 2007-07-03 | 2008-02-06 | 中国石油大学(华东) | Method for preparing load type rhodium catalyst for making high-carbon aldehyde using hydroformylation of higher olefins |
| CN101195763A (en) * | 2006-12-07 | 2008-06-11 | 中国石油化工股份有限公司 | Selective hydrogenation desulfurization transmutation method for gasoline |
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| FR2804967B1 (en) * | 2000-02-11 | 2005-03-25 | Inst Francais Du Petrole | PROCESS AND INSTALLATION USING SEVERAL CATALYTIC BEDS IN SERIES FOR THE PRODUCTION OF LOW SULFUR FUEL |
| US20060234860A1 (en) * | 2005-04-15 | 2006-10-19 | Brignac Garland B | Activating hydroprocessing catalysts using carbon monoxide |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5906730A (en) * | 1995-07-26 | 1999-05-25 | Mitsubishi Oil Co., Ltd. | Process for desulfurizing catalytically cracked gasoline |
| CN101195763A (en) * | 2006-12-07 | 2008-06-11 | 中国石油化工股份有限公司 | Selective hydrogenation desulfurization transmutation method for gasoline |
| CN101116816A (en) * | 2007-07-03 | 2008-02-06 | 中国石油大学(华东) | Method for preparing load type rhodium catalyst for making high-carbon aldehyde using hydroformylation of higher olefins |
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