WO2006114510A1 - Procede de desulfuration d'essences olefiniques - Google Patents
Procede de desulfuration d'essences olefiniques Download PDFInfo
- Publication number
- WO2006114510A1 WO2006114510A1 PCT/FR2006/000912 FR2006000912W WO2006114510A1 WO 2006114510 A1 WO2006114510 A1 WO 2006114510A1 FR 2006000912 W FR2006000912 W FR 2006000912W WO 2006114510 A1 WO2006114510 A1 WO 2006114510A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gasoline
- catalyst
- sulfur
- weight
- olefins
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including acid treatment as the refining step in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
Definitions
- cracking gasoline makes a strong contribution to sulfur and olefins in commercial gasoline.
- cracking means a cut from a coking unit, visbreaking, steam cracking or catalytic cracking (FCC) whose range of boiling points typically extends from that of hydrocarbons having 5 carbon atoms up to about 250 ° C.
- Catalytic cracking gasolines which can constitute 30 to 50% by volume of the gasoline pool, have high olefin and sulfur contents. Sulfur present in reformulated gasoline is generally attributable, more than 90%, to gasoline from catalytic cracking. The Desulphurisation of species and mainly FCC species is therefore of obvious importance for achieving standards.
- oligomerization processes have been developed to produce high octane gasolines from hydrocarbon fractions containing olefins of 3 to 6 carbon atoms. These processes use an acid catalyst which makes it possible to oligomerize the olefins present in the feedstock to isoolefins containing from 6 to 12 carbon atoms and having a high octane number. These processes produce a gasoline with high octane and sulfur free. However, these essences consist of nearly 100% by weight of olefins. There are numerous industrial processes for producing gasolines by oligomerization from olefins of 3 to 6 carbon atoms which are especially described in the book "acid-base catalysis", C. Marcilly, ed. Technip, vol2. p 475-495.
- the patent WO2005019391 proposes a process for the desulfurization of olefinic gasoline without significant loss of octane based on the production of an isolefinic species of 8 to 12 carbon atoms from a sulfur species, and the selective hydrodesulfurization of this isolefinic species to produce a desulfurized gasoline without loss of octane.
- the present invention provides a process for producing controlled sulfur and olefin fuel with the desulphurization and hydrogenation being performed with a minimized decrease in octane number.
- the invention relates to a process for the production of low sulfur content gasoline with a controlled olefin content comprising at least the following steps:
- step (ii) comprising mixing the branched olefin gasoline produced in step (i) with a gasoline rich in sulfur and olefins
- branched olefinic gasoline is a gasoline comprising at least 50% by weight of branched olefins, preferably at least 60% by weight of branched olefins and more preferably at least 65% by weight of olefins. branched. Among these branched olefins, iso-olefins are especially present, but not only.
- the invention relates to a production scheme for low sulfur gasoline with controlled olefin content.
- the gasoline produced also has a high octane number.
- a hydrocarbon fraction rich in olefins preferably containing predominantly (that is to say at least 40% by weight, preferably at least 70% by weight and very preferably at least 90% by weight), hydrocarbons having 3 to 6 carbon atoms per molecule (also referred to as C3-C6 cuts, or C3, C4, C5, C6 slice mixtures) is treated on an acid catalyst to produce a gasoline comprising a larger number of carbons, via an oligomerization reaction for example dimerization and / or trimerization. It is indeed advantageous to treat only the hydrocarbon fractions containing the shortest olefins on the acid catalyst.
- the olefinic fractions containing hydrocarbons having 7 or more carbon atoms concentrate the compounds capable of deactivating acidic catalysts, such as basic nitrogen compounds, sulfur compounds or polyunsaturated compounds.
- acidic catalysts such as basic nitrogen compounds, sulfur compounds or polyunsaturated compounds.
- olefins containing 7 or more carbon atoms form, by oligomerization, branched olefins containing more than 14 carbon atoms, which are too heavy to be incorporated into the gasoline cut.
- the branched olefinic gasoline produced by oligomerization of the olefinic fraction may contain heavy oligomerization products from trimerization reactions containing more than 12 carbon atoms.
- the separation of the C12 + heavy fraction is conventionally carried out by distillation.
- the C12 + heavy fraction can be treated in a hydrotreating or hydrogenation unit to be upgraded as a base for aviation fuel also called kerosene, or for diesel.
- the oligomerized gasoline thus obtained preferably preferably comprises hydrocarbons having 5 to 12 carbon atoms per molecule (C5-C12 cut).
- Said hydrocarbon fraction rich in olefins is preferably an olefinic gasoline comprising at least 50% by weight, preferably at least 60% by weight of olefins and more preferably at least 70% by weight of olefins.
- the olefinic feedstock treated in the oligomerization section (step i) can be derived from catalytic cracking, coking or steam-cracking units. It is generally preferable to subject the feedstock to pretreatment steps, prior to step i), in order to reduce the content of polyunsaturated compounds, sulfur compounds and nitrogen compounds. These pretreatment make it possible to maximize the cycle time of the acid catalysts.
- the diolefins present in the feed are likely to cause deactivation of the catalyst by polymerization and formation of gums.
- the polyunsaturated compounds can be extracted for recovery for petrochemical applications. This extraction is generally carried out by liquid liquid extraction or extractive distillation using polar solvents. For example, butadiene can be extracted from the C4 cut resulting from steam cracking using solvents such as acetonitrile, furfural or other polar solvents. Another possibility is to convert the diolefins to olefins by selective hydrogenation.
- the content of polyunsaturated compounds of the feedstock entering the oligomerization unit is preferably less than 1% by weight and more preferably less than 0. , 5% weight.
- Nitrogen compounds often have a basic character and thus neutralize catalytic acid sites.
- the basic compounds likely to be present in the C3 - C6 cuts are mainly amines.
- the nitrogen compounds, if they are present in said feedstock, can be extracted by a washing step with water or acid washing, or by a selective hydrogenation step as described in the patent FR 2,850,113.
- the nitrogenous compounds to be extracted are not only basic nitrogen compounds, known to deactivate acidic catalysts by neutralization of acid sites such as amines, but also non-basic nitrogen compounds such as nitriles which can also cause deactivation of acid catalysts.
- non-basic nitrogen compounds such as nitriles can also cause deactivation of acid catalysts because they can, under certain conditions be converted into basic compounds such as amines and neutralize acidic sites.
- the sulfur compounds present in the C3-C6 cuts are mainly mercaptans.
- Mercaptans can react with olefins on acid catalysts to form sulphides which are basic in nature. The sulphides thus formed can therefore degrade the activity of the acid catalysts.
- the mercaptans can be removed either by means of an extractive oxidation treatment which makes it possible to extract them in the form of disulphide such as the MEROX (registered trademark) method, or by adding addition to the olefins on a metal catalyst according to a reaction of thioetherification.
- the content of sulfur compounds in the form of mercaptans or sulphides of the olefinic feedstock of the oligomerization unit is preferably less than 100 ppm by weight, and more preferably less than 50 ppm by weight.
- the feed contains thiophene compounds and more particularly thiophene or methylthiophenes
- these compounds are capable of reacting with a fraction of the olefins present in the C3-C6 olefinic cut to form heavier alkylated thiophene compounds.
- These compounds can therefore optionally be removed from the branched olefinic gasoline by simple distillation.
- the catalysts used in stage i) are acid catalysts preferably chosen from the group consisting of: supported inorganic acids such as phosphoric acids on silica, sulfonic acids on polymers such as ion exchange resins, oxides minerals such as aluminas, amorphous silica-alumina, zeolites.
- the compounds that are to be produced must be branched to maximize their octane number.
- acid catalysts having a mean pore diameter large enough to allow the diffusion of highly branched molecules.
- the acid catalyst used preferably has an average pore diameter greater than 0.5 nm and more preferably greater than 0.7 nm.
- An amorphous silica-alumina type catalyst or an ion exchange resin is preferably used.
- the catalyst is amorphous silica-alumina
- the reactor is operated at a temperature of between 50 ° C. and 250 ° C., a WH of between 0.5 h -1 and 5 h -1, and a pressure such that the reaction mixture is maintained in the liquid phase in the reactor.
- the branched olefinic gasoline from the oligomerization step contains more than 90% by weight of olefins. In order to reduce the olefin content, this gasoline must be partially hydrogenated. It has been found that it is particularly advantageous to hydrogenate this gasoline and preferably the C5-C12 fraction together with the desulphurization of sulfur-rich cracking gasoline and olefins.
- the branched olefinic gasoline is thus mixed with the cracking gasoline that is to be desulphurized (step ii).
- the joint treatment of branched olefin gasoline and cracking gasoline makes it possible to treat the two gasoline bases in the same reaction section, which limits the investments to be made in the refinery. Moreover, it has surprisingly been found that the joint treatment of these two sections makes it possible to limit the octane loss associated with the hydrogenation of the olefins during the hydrodesulfurization and hydrogenation stage.
- the mixture consisting of branched olefinic gasoline and cracking gasoline is therefore treated in a hydrodesulfurization step (step iii).
- this mixture comprises at least 5% by weight of branched olefinic gasoline, more preferably at least 10% by weight of branched olefinic gasoline and very preferably at least 15% by weight of branched olefinic gasoline with respect to sum of the two essences.
- the hydrodesulfurization step is carried out by contacting the mixture of gasoline to be treated with hydrogen on a catalyst capable of converting the organic sulfur compounds into H 2 S. It is however advantageous to use a catalyst and operating conditions making it possible to control the degree of hydrogenation of the olefins according to a process known as selective hydrodesulfurization.
- the operating conditions of the hydrodesulfurization reactor are those typically used to selectively desulphurize olefinic species.
- the operation is carried out, for example, at a temperature of between 220 ° C. and 350 ° C., under a pressure preferably of between 0.1 and 5 MPa, more preferably between 1 MPa and 3 MPa.
- the space velocity is preferably between about 0.5 h -1 and 20 h -1 (expressed as the volume of liquid gas to be desulfurized per volume of catalyst per hour), and more preferably between 1 h -1 and 10 h -1 and very preferably between 2 h -1 and 8 h -1 .
- the ratio of the hydrogen flow rate on the gasoline flow to be desulphurized is preferably between 50 liter / liter and 800 liter / liter, and more preferably between 100 liter / liter and 400 liter / liter.
- the hydrodesulfurization reactor contains at least one hydrodesulfurization catalyst which preferably comprises at least one group VIII element and a group VIb element, deposited on a porous support.
- the group VIII element is preferably iron, cobalt or nickel.
- the group VIb element is preferably molybdenum or tungsten.
- the content of group VIII element expressed as oxide is preferably between 0.5% by weight and 15% by weight and more preferably between 0.7% by weight and 10% by weight.
- the metal content of group VIb is preferably from 1.5% by weight to 60% by weight and more preferably from 2% by weight to 50% by weight.
- the porous support is preferably selected from the group consisting of: silica, alumina, silicon carbide or a mixture of these constituents.
- a support comprising alumina, preferably at least 70% by weight of alumina, more preferably at least 80% by weight of alumina, the specific surface area of which is less than 200 m 2 / g, preferably less than 150 m 2 / g, and very preferably less than 100 m 2 / g.
- the porosity of the catalyst before sulfurization is preferably such that the average pore diameter is greater than 20 nm and more preferably between 20 and 100 nm.
- the surface density of the Group VIb metal is preferably between 2.10 "and 40.10 4" 4 gram of oxide of said metal per m 2 of support, more preferred between 4.10 "and 16.10 4" 4 g / m 2.
- the catalyst generally undergoes a sulphurization step before it is brought into contact with the feedstock to be treated.
- this sulphurization is obtained by a heat treatment of the solid during which it is brought into contact with a decomposable sulfur compound and hydrogen sulphide generator.
- the catalyst can be directly contacted with a gas stream comprising hydrogen sulphide. This step may be carried out ex situ or in situ, ie inside or outside the hydrodesulfurization reactor.
- the sulfurized catalyst is also subjected to a carbon deposition step so as to deposit a significant carbon content, preferably less than or equal to 2.8% by weight.
- This carbon deposition step aims at improving the selectivity of the catalyst by preferentially poisoning the hydrogenating activity of the catalyst. Very preferably the carbon content deposited is between 0.5 and 2.6% by weight. This carbon deposition step may be carried out before, after, or during the step of sulphurizing the catalyst.
- the selective hydrodesulfurization can be carried out in a reactor comprising a catalyst as described previously in this application. However, it may be advantageous to carry out this step using a sequence of several catalysts and possibly in several reactors.
- the group VIII element content is preferably between 1 and 60% by weight and more preferably between 2 and 20% by weight.
- the metal is introduced as a metal oxide, then it is sulphurized before use.
- This finishing step is mainly carried out to decompose saturated sulfur compounds such as mercaptans or sulphides, which are contained in the effluent of a first desulfurization step. When present, the finishing step is preferably carried out at a temperature higher than the first desulfurization step.
- the finishing step may be carried out on a hydrodesulfurization catalyst which comprises at least one at least one Group VIII element and one Group VIb element, deposited on a porous support.
- the group VIII element is preferably iron, cobalt or nickel.
- the group VIb element is preferably molybdenum or tungsten.
- the element content of group VIIl, expressed as oxide, is preferably between 0.5% by weight and 10% by weight, and more preferably between 0.7% by weight and 5% by weight.
- the Group VIb metal content is preferably between 1.5 wt.% And 50 wt.% And more preferably between 2 wt.% And 20 wt.%.
- the porous support is preferably selected from the group consisting of. silica, alumina, silicon carbide or a mixture of these constituents.
- silica alumina
- alumina-based support whose specific surface area is less than 200 m 2 / g, preferably less than 150 m 2 / g, and very preferably lower at 100 m 2 / g.
- the porosity of the catalyst before sulfurization is preferably such that the average pore diameter is greater than 20 nm and preferably between 20 and 100 nm.
- the surface density of the Group VIb metal is preferably between 2.10 "and 40.10 4" 4 gram of oxide of said metal per m 2 of support, preferably between 4.10 "and 16.10 4" 4 g / m 2.
- the catalyst of this finishing step preferably has a catalytic activity of between 1% and 90%, indeed between 1% and 70%, and preferably between 1% and 50% of the catalytic activity of the main hydrodesulfurization catalyst. (step iii), measured in terms of conversion.
- this finishing step is preferably carried out at a temperature above the temperature of the main desulfurization step.
- the desulfurization steps are generally carried out in fixed catalyst bed reactors which may comprise several catalyst beds separated by a cold fluid injection zone called a cooling zone for controlling the temperature rise along the reactor.
- the gasoline is cooled and condensed.
- L 1 H 2 S resulting from the transformation of the organic sulfur compounds is separated with the excess of hydrogen from the gasoline (step iv).
- L 1 H 2 S dissolved in the gasoline is preferably removed by stripping.
- EXAMPLE 1 (Comparative): a) Production of a branched gasoline: An olefinic C4 cut designated ⁇ 1 from a catalytic cracking unit whose characteristics are shown in Table 1 is treated with an acidic catalyst composed of a silica-alumina amorphous marketed by Axens under the reference IP 501. In addition, this cut contains 3 ppm of sulfur and 1 ppm of nitrogen.
- the operating conditions are as follows: the temperature is 140 ° C., the VVH is 1 h -1 and the pressure is 6 MPa. The product of the reaction is distilled to recover dimers and trimers containing 6 to 12 carbon atoms from the reaction of butenes.
- the gasoline thus produced called ⁇ 2 contains more than 90% by weight of olefins, more than 90% by weight of which are branched olefins, and has an octane number calculated by averaging the engine octane number and the research octane number of 90.1. This average is usually called FON.
- This species is therefore a branched olefinic species as described in the invention. Table 1
- This essence ⁇ 2 is hydrogenated according to a hydrogenation process not according to the invention, in the presence of a hydrogenation catalyst containing nickel deposited on alumina, in order to hydrogenate a fraction of the olefins and to be able to incorporate gasoline thus hydrogenated in a mixture of commercial gasoline, the overall olefin content is limited to 18%.
- the ⁇ 3 gasoline obtained after partial hydrogenation contains 45% by volume of olefins and has a FON octane number of 90.5. Hydrogenation of olefinic gasoline therefore has little effect on the octane number.
- the gasoline is desulphurised under the following conditions: the temperature is 280 ° C., the pressure of 2 MPa, the VVH of 3 h -1, and the ratio of the flow rate of hydrogen to the flow rate of gasoline to be desulphurized is 300 liters per liter.
- the ⁇ 2 desulfurized gasoline produced contains 12 ppm of sulfur, 19.8% of olefins and its FON octane number is 82.2.
- the gasoline ⁇ 1 thus produced contains 26.1% olefin volume, 10 ppm sulfur and has a FON octane number of 84.2.
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN2006800141200A CN101233214B (zh) | 2005-04-28 | 2006-04-24 | 烯烃汽油的脱硫方法 |
EP06743731A EP1879983A1 (fr) | 2005-04-28 | 2006-04-24 | Procede de desulfuration d'essences olefiniques |
US11/912,587 US20090101545A1 (en) | 2005-04-28 | 2006-04-24 | Method for Desulfurising Olefin Motor Gasoline |
BRPI0607668A BRPI0607668B1 (pt) | 2005-04-28 | 2006-04-24 | processo de dessulfuração de gasolinas olefínicas |
JP2008508256A JP5149157B2 (ja) | 2005-04-28 | 2006-04-24 | オレフィンガソリンの脱硫方法 |
KR1020077027660A KR101286872B1 (ko) | 2005-04-28 | 2006-04-24 | 올레핀계 가솔린의 탈황 방법 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0504302A FR2885137B1 (fr) | 2005-04-28 | 2005-04-28 | Procede de desulfuration d'essences olefiniques |
FR0504302 | 2005-04-28 |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2006114510A1 true WO2006114510A1 (fr) | 2006-11-02 |
WO2006114510B1 WO2006114510B1 (fr) | 2006-12-28 |
Family
ID=35149634
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2006/000912 WO2006114510A1 (fr) | 2005-04-28 | 2006-04-24 | Procede de desulfuration d'essences olefiniques |
Country Status (8)
Country | Link |
---|---|
US (1) | US20090101545A1 (fr) |
EP (1) | EP1879983A1 (fr) |
JP (1) | JP5149157B2 (fr) |
KR (1) | KR101286872B1 (fr) |
CN (1) | CN101233214B (fr) |
BR (1) | BRPI0607668B1 (fr) |
FR (1) | FR2885137B1 (fr) |
WO (1) | WO2006114510A1 (fr) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
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CN102879522B (zh) * | 2011-07-11 | 2016-01-13 | 中国石油化工股份有限公司 | 测定加氢脱硫反应产物中有机硫的方法 |
US10144883B2 (en) | 2013-11-14 | 2018-12-04 | Uop Llc | Apparatuses and methods for desulfurization of naphtha |
US10308883B2 (en) | 2015-10-07 | 2019-06-04 | Axens | Process for desulfurizing cracked naphtha |
KR102581907B1 (ko) * | 2018-01-02 | 2023-09-22 | 에스케이이노베이션 주식회사 | 파라핀을 제조하는 방법 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2005019391A1 (fr) * | 2003-08-19 | 2005-03-03 | Exxonmobil Research And Engineering Company | Desulfurisation de naphta sans perte d'octane et avec retention d'olefines accrue |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3914817C2 (de) * | 1989-05-05 | 1995-09-07 | Huels Chemische Werke Ag | Verfahren zur Oligomerisierung von Olefinen |
US6013598A (en) * | 1996-02-02 | 2000-01-11 | Exxon Research And Engineering Co. | Selective hydrodesulfurization catalyst |
US6231753B1 (en) * | 1996-02-02 | 2001-05-15 | Exxon Research And Engineering Company | Two stage deep naphtha desulfurization with reduced mercaptan formation |
US5863419A (en) * | 1997-01-14 | 1999-01-26 | Amoco Corporation | Sulfur removal by catalytic distillation |
CA2407035A1 (fr) * | 2000-04-24 | 2001-11-01 | Catalytic Distillation Technologies | Procede de production de stocks d'essence |
FR2821852B1 (fr) * | 2001-03-12 | 2003-05-02 | Inst Francais Du Petrole | Procede de production d'une essence desulfuree a partir d'une coupe essence contenant de l'essence de conversion |
US7297251B2 (en) * | 2002-05-21 | 2007-11-20 | Exxonmobil Research And Engineering Company | Multi-stage hydrodesulfurization of cracked naphtha streams with a stacked bed reactor |
FR2850299B1 (fr) * | 2003-01-29 | 2006-12-01 | Inst Francais Du Petrole | Catalyseurs partiellement cokes utilisables dans l'hydrotraitement des coupes contenant des composes soufres et des olefines |
-
2005
- 2005-04-28 FR FR0504302A patent/FR2885137B1/fr active Active
-
2006
- 2006-04-24 CN CN2006800141200A patent/CN101233214B/zh active Active
- 2006-04-24 KR KR1020077027660A patent/KR101286872B1/ko active IP Right Grant
- 2006-04-24 JP JP2008508256A patent/JP5149157B2/ja active Active
- 2006-04-24 US US11/912,587 patent/US20090101545A1/en not_active Abandoned
- 2006-04-24 WO PCT/FR2006/000912 patent/WO2006114510A1/fr active Application Filing
- 2006-04-24 BR BRPI0607668A patent/BRPI0607668B1/pt active IP Right Grant
- 2006-04-24 EP EP06743731A patent/EP1879983A1/fr not_active Withdrawn
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2005019391A1 (fr) * | 2003-08-19 | 2005-03-03 | Exxonmobil Research And Engineering Company | Desulfurisation de naphta sans perte d'octane et avec retention d'olefines accrue |
Also Published As
Publication number | Publication date |
---|---|
EP1879983A1 (fr) | 2008-01-23 |
BRPI0607668A2 (pt) | 2009-09-22 |
FR2885137A1 (fr) | 2006-11-03 |
KR101286872B1 (ko) | 2013-07-16 |
US20090101545A1 (en) | 2009-04-23 |
CN101233214B (zh) | 2013-01-02 |
JP5149157B2 (ja) | 2013-02-20 |
BRPI0607668B1 (pt) | 2015-11-03 |
CN101233214A (zh) | 2008-07-30 |
FR2885137B1 (fr) | 2007-07-13 |
JP2008539296A (ja) | 2008-11-13 |
WO2006114510B1 (fr) | 2006-12-28 |
KR20080007265A (ko) | 2008-01-17 |
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