MANUFACTURING PROCESS OF ALCOHOLIC ESTERS FROM TRIGLYCERIDES AND ALCOHOLS BY HETEROGENEOUS CATALYSTS IN CONNECTION WITH AT LEAST ONE CELEBRATIONS SOLUTION OF ZNAL2O3+X AND ZNO

PROCEDURE FOR THE UTILIZATION A HYDROCARBON EMPLOYMENT AND REDUCTION OF THE STEAM PRESSURE OF THIS EMPLOYMENT

METHOD FOR DEHYDRATING ALCOHOLS TO OBTAIN OLEFINS, INVOLVING A STEP OF CATALYST SELECTIVATION

L'invention concerne un procédé de déshydratation des alcools en oléfines comprenant une étape réactionnelle et une étape de sélectivation du catalyseur.

LOW-ENERGY CONSUMPTION METHOD FOR DEHYDRATING ETHANOL INTO ETHYLENE

L'invention décrit un procédé de déshydratation d'une charge éthanol en éthylène comprenant la vaporisation de ladite charge éthanol en mélange avec au moins une partie du flux d'eau purifié recyclé selon l'étape f) dans un échangeur grâce à un échange de chaleur avec l'effluent issu du dernier réacteur, ledit mélange étant introduit dans ladite étape de vaporisation à une pression comprise entre 0,1 et 0,4 MPa, la compression du mélange vaporisé dans un compresseur, l'introduction du mélange vaporisée et comprimée, à une température d'entrée comprise entre 350 et 500°C et à une pression d'entrée comprise entre 0,2 et 1,3 MPa, dans au moins un réacteur adiabatique contenant au moins un catalyseur de déshydratation et dans lequel la réaction de déshydratation a lieu, la séparation de l'effluent issu du dernier réacteur adiabatique de l'étape c) en un effluent comprenant de l'éthylène à une pression inférieure à 1 MPa et un effluent comprenant de l'eau, la purification d'au moins une partie ...

PROCESS Of IMPROVEMENT OF CUTS GASOLINES AND TRANSFORMATION INTO COMPLEMENTARY GAZOLESAVEC TREATMENT ALLOWING TO INCREASE the OUTPUT Of the COUPEGAZOLE

PROCESS OF TREATMENT Of C4 HYDROCARBONS COMPRISING OF BUTADIENE AND ACETYLENIC DESCOMPOSES INCLUDING/UNDERSTANDING OF the STAGES OF DISTILLATION AND HYDROGENATIONSELECTIVE

PROCESS OF DESULPHURIZATION Of an EFFLUENT OF CRACKING, OR STEEMCRAQUAGE OUCOKING

PROCEEDED OF DIRECT CONVERSION Of a LOAD INCLUDING/UNDERSTANDING OF OLEFINS HAS QUATREET/OU FIVE ATOMS OF CARBON, FOR the PRODUCTION OF PROPYLENE WITH GASOLINE UNECO-PRODUCTION

L'invention concerne un procédé de production de propylène à partir d'une coupe C4/C5 oléfinique (par exemple de vapocraquage et/ou de craquage catalytique), ce procédé comprenant une hydrogénation sélective optionnelle, une oligomérisation sélective des isobutènes et un oligocraquage des n-butènes.L'invention permet d'obtenir une conversion élevée avec un bon rendement en propylène et de maximiser la production d'essence de bonne qualité. The invention relates to a process for producing propylene from an olefinic C4 / C5 cut (for example steam cracking and / or catalytic cracking), which process comprises optional selective hydrogenation, selective oligomerization of isobutenes and oligocracking of The invention achieves high conversion with good propylene yield and maximizes the production of good quality gasoline.

PROCESS OF TERTIARY PRODUCTION Of OLEFIN BY DECOMPOSITION Of ALKYLIC ETHER TERTIARY

Procédé de production d'oléfine tertiaire par décomposition d'éther alkylique tertiaire comprenant a) la décomposition d'au moins un éther en un produit contenant un alcool et une oléfine tertiaire, b) le fractionnement d'au moins une partie du produit issu de a) dans une zone de fractionnement (C1) permettant d'obtenir d'une part de l'oléfine tertiaire et d'autre part de l'alcool, c) la purification d'au moins une partie de l'oléfine tertiaire obtenue à l'étape b) dans laquelle ladite partie est envoyée dans une zone d'extraction (L1) par lavage à l'eau à partir de laquelle on récupère une fraction (D) contenant l'oléfine tertiaire, et d) et une étape dans laquelle au moins une partie de la fraction (D) issue de c) est envoyée dans une zone de séparation (Co) à partir de laquelle on récupère une fraction liquide aqueuse (Le) et une fraction liquide hydrocarbonée (Lc) contenant la majeure partie de l'oléfine tertiaire.

VALVE PLATE FOR DISTRIBUTING A GASEOUS AND LIQUID PHASES

The invention relates to an enclosure, a column and a reactor comprising a device for mixing and distributing at least one gaseous phase and at least one liquid phase. Said device is arranged upstream of a reaction or gas/liquid contact area which can consist of a lining bed or a bed made of solid possibly catalytic particles. A method for using the inventive enclosure and a method for the production thereof are also disclosed. © KIPO & WIPO 2007 ...

Device for mixing and distributing a dense fluid and a light fluid, placed upstream from a granular bed, and its use in descending flow

Device for mixing and distributing a dense, generally liquid, fluid and a light, generally gaseous, fluid, placed in a reaction chamber upstream from a granular bed ( 70 ) or between two successive granular beds, the said device being characterized by a tubular system ( 50 ) for the introduction of dense fluid from outside the reactor, up to a level lower than the level of establishment of the interface between the dense fluid and the light fluid, situated above the plate and preferably more or less next to that of the plate ( 62 ). Application of this device to any type of gas/liquid reaction in a fixed bed in particular for hydrotreatment.

Verfahren zur Herstellung von tertiären Olefinen durch Spaltung von tertiären Alkylethern in dem die erste Reinigungsstufe eine Wäsche mit Wasser ist

Verfahren zur Verbesserung von Benzinschnitten und zur Umwandlung zu Gasölen

Method for direct conversion of a feedstock comprising C4/C5 olefins for producing propylene with co-production of gasoline

PROCEDURE FOR THE TRANSFORMATION OF ETHANOL INTO A COMPONENT FOR DIESEL FUEL

OLIGOMERISIERUNGSVERFAHREN FROM OLEFINEN WITH THE HELP OF A CATALYST ON SILICON ALUMINUM BASIS

PROCESS FOR PRODUCING ALCOHOLS WITH CLOSTRIDIUM ON A SOLID SUPPORT

La présente invention concerne un procédé de production en d'alcools, dans lequel on introduit en un fluide sucré dans un réacteur fermentaire (2) pour produire un moût fermentaire enrichi en isopropanol, butanol, éthanol et acétone par rapport au fluide sucré, le réacteur fermentaire (2) comprenant une biomasse produite par une souche appartenant au genre Clostridium supportée sur un support solide (9) comprenant une mousse de polyuréthane; et un réacteur fermentaire (2) comprenant ladite biomasse supportée sur ledit support solide (9).

PROCESS FOR THE PREPARATION OF ESTER ALCOHOLS FROM TRIGLYCERIDES AND ALCOHOLS EMPLOYING HETEROGENEOUS CATALYSTS COMPRISING AT LEAST ONE SOLID SOLUTION OF ZNXAL2O3+X AND ZNO

Un procédé de préparation d'une composition d'esters alcooliques d'acides monocarboxyliques linéaires de 6 à 26 atomes de carbone à partir d'une huile végétale ou animale, neutre ou acide, vierge ou recyclée, avec des monoalcools de 1 à 18 atomes de carbone, en présence d'un catalyseur associant au moins une solution solide de type Zn x Al2O(3+x) dans laquelle x est compris entre 0 et 1 (bornes exclues) et du ZnO libre présent entre 7 et 30% en masse permet d'obtenir directement, en une ou plusieurs étapes, un ester utilisable comme carburant ou combustible et une glycérine pure.

PROCESS FOR DEHYDRATION AND ISOMERIZATION OF C4 ALCOHOLS USING AN AMORPHOUS SOLID WITH SUITABLE POROSITY

La présente invention a pour objet un procédé de production d'oléfines en C4, à partir d'une charge de monoalcool en C4 dans lequel on réalise une réaction de déshydratation du monoalcool en au moins une oléfine, et une réaction d'isomérisation squelettale d'au moins une des oléfines produites dans une même enceinte réactionnelle, en présence d'un catalyseur à base d'alumine à porosité adaptée.

METHOD FOR PRODUCING ETHYLENE OXIDE FROM A THERMO-MECHANICALLY INTEGRATED ETHANOL STREAM

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène puis d'oxydation de l'éthylène en oxyde d'éthylène comprenant une étape de vaporisation d'une charge comprenant ladite charge éthanol et au moins une partie d'un flux d'eau de dilution comprenant de l'éthanol recyclé de manière à produire une charge vaporisée, une étape de compression dans un compresseur entraîné par une turbine à condensation entraînée par la vapeur générée par l'étape d'oxydation, une étape de déshydratation d'un mélange comprenant ladite charge vaporisée comprimée, une étape de séparation de l'effluent issu de l'étape de déshydratation en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau, une étape de purification d'au moins une partie de l'effluent comprenant de l'eau et la séparation en au moins un flux d'eau traitée et un flux d'eau de dilution comprenant de l'éthanol, ce dernier étant recyclé en amont de l'étape de vaporisation, et une étape d'oxydation de l'éthylène ...

PROCESS OF DESULPHURIZATION Of an EFFLUENT OF CRACKING

REACTIONAL ZONE COMPRISING TWO RISERS IN PARALLEL AND A ZONE OF SOLID SEPARATION GAS COMMUNE FOR THE PRODUCTION OF PROPYLENE

La présente invention décrit une zone réactionnelle comportant au moins deux réacteurs fluidisés, l'un principal pour le craquage d'une coupe hydrocarbonée lourde, l'autre additionnel pour le craquage d'une ou plusieurs coupes légères, les effluents des deux réacteurs étant traités dans une zone de séparation gaz solide et de trempe commune. II en résulte un niveau de performances accru grâce à un contrôle optimisé des réactions de dégradation thermique dans la zone réactionnelle.

Alternate metathesis of olefins

La présente invention concerne un procédé pour effectuer en continu la réaction de métathèse ou de disproportionation des oléfines comprenant au moins 2 phases, une phase a) de réaction dans une zone comprenant au moins un réacteur contenant au moins un catalyseur en lit fixe et une phase b) de régénération dans une zone comprenant au moins un réacteur contenant au moins un catalyseur en lit fixe caractérisé en ce qu'alternativement au moins un réacteur passe d'une phase à l'autre. Suivant la figure 1, la charge contenant les oléfines traverse le réacteur R1 selon un mode à flux ascendant. La charge à traiter contenant les oléfines est introduite dans le réacteur R1 par la ligne 1a. Dans ce réacteur, les oléfines contenues dans la charge subissent une métathèse ou une disproportionation, puis l'effluent sort du circuit par la ligne 11. Simultanément le réacteur R2 est placé en phase de régénération de son catalyseur, les différents gaz de régénération sont introduits dans le réacteur R2 ...

Transformation of hydrocarbon charge to give fraction with improved octane index and one with improved cetane index, comprises selective etherification and oligomerization

On décrit un procédé de transformation d'une charge initiale d'hydrocarbures comprenant de 4 à 15 atomes de carbone, bornes incluses, en une fraction d'hydrocarbures présentant un indice d'octane amélioré et une fraction d'hydrocarbures à fort indice de cétane.

PROCESS Of IMPROVEMENT OF CUTS GASOLINES AND TRANSFORMATION INTO COMPLEMENTARY GAZOLESAVEC TREATMENT ALLOWING TO INCREASE the OUTPUT Of the COUPEGAZOLE

L'invention concerne un procédé de transformation d'une charge hydrocarbonée de type essence en une coupe essence de nombre d'octane supérieur à celui de la charge, et une coupe gazole d'indice de cétane supérieur à 45 comprenant les étapes suivantes: a) une étape de séparation par membrane (B) de la charge hydrocarbonée dans des conditions permettant la séparation sélective de la majorité des oléfines linéaires présentes dans ladite charge et constituant la coupe β, la coupe contenant la majorité des oléfines ramifiées, dite coupe γ, constituant une essence à fort indice d'octane, supérieur à celui de la charge. b) une étape d'oligomérisation (C) des oléfines linéaires (coupe β) contenues dans les effluents issus de l'étape de séparation sur membrane (B) dans des conditions d'oligomérisation modérées, c) une étape de séparation par distillation (D) des effluents issus de l'étape d'oligomérisation en au moins deux coupes, d) une étape d'hydrogénation (E) d'une des coupes obtenue à l'étape ...

A new two-stage isomerization process for 8C aromatic compounds to produce paraxylene and orthoxylene

Procédé d'isomérisation d'une charge contenant des composés aromatiques à 8 atomes de carbone comprenant une étape d'isomérisation effectuée au moyen d'un catalyseur contenant au moins une zéolithe de type structural EUO et au moins un métal du groupe VIII et une étape de déshydrogénation. Selon la figure 1, la charge à traiter est introduite dans la zone d'isomérisation R1 par la ligne 1. De l'hydrogène sensiblement pur est introduit dans la ligne 1 par la ligne 12 et de l'hydrogène recyclé est introduit dans la ligne 1 par la ligne 13. Une purge de l'hydrogène qui circule dans la ligne 13 est effectuée par la ligne 15. L'effluent de la zone d'isomérisation R1 est envoyé dans une zone de séparation S1 par la ligne 2. Dans S1, l'hydrogène contenu dans l'effluent est isolé et recyclé vers l'entrée de la zone d'isomérisation R1 par la ligne 13, le reste de l'effluent est évacué de cette zone de séparation S1 par la ligne 3. Le fluide contenu dans la ligne 3 est chauffé dans un four F1 puis ...

PROCEEDED OF SEPARATION OF PROPANE AND PROPYLENE IMPLEMENTING A FRACTIONATING COLUMN AND A UNIT OF SEPARATION PER MEMBRANE

Procédé de séparation du propane et du propylène mettant en oeuvre une colonne à distiller et au moins une unité de séparation par membrane constituée d'un ou plusieurs modules travaillant en série, ladite unité de séparation par membrane étant placée soit en amont, soit en aval, soit en amont et en aval de la colonne à distiller.

Desulfurization of charge containing thiophene or thiophenic components

Desulfurization of a charge containing thiophene or thiophenic components comprises eliminating the diolefins in the charge, fractionating the charge in a distillation zone into a heavy fraction which is then desulfurized and a lighter fraction including the thiophene and/or thiophenic components, and alkylating the thiophene and/or thiophenic components using at least one olefin Preferred Features: The alkylated products are recycled to the distillation zone to be included in the heavy fraction, or are sent directly to be included in the heavy fraction. The olefin used is present on at least one tray in the distillation zone. The charge is catalytic cracking effluent or vapor cracking effluent. The alkylation catalyst is zeolites, silica- aluminas or ion exchange resins. Desulfurizing with boiling points below 350 deg C, containing 3-90 wt.% olefins, and 5 ppm and 3 wt.% sulfur comprises the use of at least one distillation unit, at least one alkylation unit and at least one hydrotreatment unit. The distillation can be before or during the alkylation and the hydrotreatment is after the distillation. The sulfur components are alkylated on an acid catalyst in the presence of olefins with 2-10 carbon atoms, with the molecular ratio of olefin to sulfur being 0.1-1000 moles per mole, preferably 0.5-500 moles per mole. The alkylation unit operates at a pressure of at least 5 bars. Nitrous components are at least partially removed from the charge before alkylation, upstream or downstream of the distillation.

PROCESS FOR THE PRODUCTION OF MIDDLE DISTILLATES FROM A FEEDSTOCK COMPRISING BUTANOL AND PENTANOL

The invention relates to a process for the production of middle-distillate hydrocarbon-containing bases from a feedstock comprising butanol and pentanol, with said process comprising at least: a) Isomerizing dehydration of said feedstock; b) Separation of the water that is present in said olefinic effluent; c) Purification of the organic liquid effluent coming from b); d) Selective oligomerization of a feedstock that comprises at least a portion of the purified organic effluent coming from c), to produce a first oligomerization effluent; e) Oligomerization of said first oligomerization effluent in such a way as to produce a second oligomerization effluent; f) Fractionation of said second oligomerization effluent into at least three products, a light product, an intermediate product and a distillate product; g) Oligomerization of at least a portion of said intermediate product; h) Hydrogenation of at least a portion of said distillate product.

Method for direct conversion of a feedstock comprising olefins with four and/or five carbo atoms for producing propylene with co-production of gasoline

The invention concerns a method for producing propylene from a C4/C5 olefinic cut (for example steam cracking and/or catalytic cracking), said method including optional selective hydrogenation, selective oligomerization of isobutylenes and oligomeric cracking of n-butylenes. The invention provides for high conversion with a good yield in propylene and maximization of good quality gasoline production.

SEPARATION IMPROVEMENT IN A PROCEDURE FOR THE PRODUCTION FROM ACRYLIC ESTERS PFLANZENODER ANIMAL OILS AND AN ALIPHATIC MONO ALCOHOL

Process for producing alcohols with clostridium on a solid support

The present invention relates to a process for producing alcohols, in which a sweetened fluid is introduced into a fermentation reactor (2) in order to produce a fermenting wort enriched in isopropanol, butanol, ethanol and acetone with respect to the sweetened fluid, the fermentation reactor (2) comprising a biomass produced by a strain belonging to the genus ...

METHOD FOR TREATING AN ALCOHOL FEEDSTOCK FOR THE PRODUCTION OF OLEFINS

L'invention concerne un procédé de traitement d'une charge alcoolique comprenant : a) une étape de préchauffe de ladite charge alcoolique à une température comprise entre 70°C et 200°C; b) une étape de prétraitement sur un solide acide, opérant à une température comprise entre 70°C et 200°C, pour produire une charge alcoolique prétraitée; c) une étape de vaporisation partielle pour produire un flux vaporisé et un flux liquide; et d) une étape de purification du flux liquide issu de l'étape c), en un flux riche en eau, un flux riche en mono-alcool et un flux riche en impuretés.

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND ISOPROPANOL

L'invention se rapporte à un procédé de production d'un mélange d'éthylène et de propylène à partir d'un mélange contenant de l'ethanol, de l'isopropanol et ayant une teneur en eau comprise entre 30 et 75% poids par rapport au poids total du mélange, dans lequel: a) on met en contact dans une unité de déshydratation le mélange avec un catalyseur de déshydratation choisi parmi: une alumine (A) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 200 et 350 m2/g, un diamètre moyen mésoporeux compris entre 5 et 15 nm, une teneur en sodium inférieure à 50 ppm poids et une teneur en soufre inférieure à 40 ppm poids; et une alumine (B) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 130 et 180 m2/g, un diamètre moyen mésoporeux compris entre 14 et 20 nm, une teneur en sodium comprise entre 300 et 600 ppm poids et une teneur en soufre comprise entre 800 et 1300 ppm poids; la mise en contact étant effectuée à une température ...

METHOD FOR PRODUCING ETHYLENE OXIDE FROM A THERMALLY INTEGRATED ETHANOL STREAM

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène puis d'oxydation de l'éthylène en oxyde d'éthylène comprenant une étape de vaporisation d'une charge comprenant ladite charge éthanol et au moins une partie d'un flux d'eau de dilution comprenant de l'éthanol recyclé de manière à produire une charge vaporisée, une étape de déshydratation d'un mélange comprenant ladite charge vaporisée et un flux vaporisé d'eau de dilution comprenant de l'éthanol, une étape de séparation de l'effluent issu de l'étape de déshydratation en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau, une étape de purification d'au moins une partie de l'effluent comprenant de l'eau et la séparation en au moins un flux d'eau traitée et un flux d'eau de dilution comprenant de l'éthanol, une étape de recyclage et de vaporisation d'au moins une partie du flux d'eau de dilution comprenant de l'éthanol issu de l'étape de séparation par vaporisation partielle ou totale dans ...

METHOD FOR PRODUCING ETHYLENE OXIDE FROM A THERMO-MECHANICALLY INTEGRATED ETHANOL STREAM

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène puis d'oxydation de l'éthylène en oxyde d'éthylène comprenant une étape de vaporisation d'une charge comprenant ladite charge éthanol et au moins une partie d'un flux d'eau de dilution comprenant de l'éthanol recyclé de manière à produire une charge vaporisée, une étape de compression dans un compresseur entraîné par une turbine à condensation entraînée par la vapeur générée par l'étape d'oxydation, une étape de déshydratation d'un mélange comprenant ladite charge vaporisée comprimée, une étape de séparation de l'effluent issu de l'étape de déshydratation en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau, une étape de purification d'au moins une partie de l'effluent comprenant de l'eau et la séparation en au moins un flux d'eau traitée et un flux d'eau de dilution comprenant de l'éthanol, ce dernier étant recyclé en amont de l'étape de vaporisation, et une étape d'oxydation de l'éthylène ...

PROCEEDED Of ISOMERIZATION OF COMPOSE AROMATIC HAS EIGHT CARBON ATOMS ENDEUX SUCCESSIVE STAGES AND USING a CATALYST ACTIVE

PROCESS OF PRODUCTION OF PROPYLENE IN THE PRESENCE OF A MACROPOROUS CATALYST SE PRESENTING IN THE FORM OF SPHERICAL BALLS

DEVICE OF DISTRIBUTION MAKING IT POSSIBLE TO CARRY OUT A POLYPHASE MIXTURE AND ENGINE ASSOCIATES

Dispositif permettant de réaliser une distribution et un mélange polyphasique entre deux fluides comportant une chambre dédiée au passage d'un premier fluide, ladite chambre étant percée de tubes ou cheminées perforés servant au passage à travers la chambre d'un deuxième fluide dans un état physique différent du premier ou non miscible avec le premier, lesdits tubes étant percées par au moins un orifice permettant le passage du premier fluide et le mélange entre les fluides à travers les tubes. Le deuxième fluide est injecté en amont dudit dispositif et l'injection du premier fluide est effectuée au niveau dudit dispositif.

PROCESS Of OLIGOMERIZATION OF OLEFINS USING a CATALYST Containing SILICE-ALUMINE.

On décrit un procédé d'oligomérisation d'une charge hydrocarbonée oléfinique consistant en la mise en contact de ladite charge avec un catalyseur comprenant une silice - alumine, la teneur massique en silice dudit catalyseur étant comprise entre 5 et 95% poids, ledit catalyseur étant préparé selon un procédé comprenant au moins :a) le mélange d'au moins un composé aluminique partiellement soluble en milieu acide avec soit au moins un composé silicique totalement soluble dans le mélange réactionnel soit une combinaison formée d'au moins un composé silicique et d'au moins un composé aluminique, lesdits composés silicique et aluminique étant totalement solubles dans le mélange réactionnel, de manière à former un solide précurseur dudit catalyseurb) le traitement hydrothermal, pendant une durée d'au moins 3 heures, du solide issu de ladite étape a).

METHOD OF PREPARATION Of a DIESEL CUT BY OLIGOMERIZATION

La présente invention porte sur un procédé de préparation d'une coupe diesel qui comprend les étapes successives suivantes : 1) une oligomérisation d'une coupe d'hydrocarbures oléfiniques en C2-C12, de préférence en C3-C7 et plus préférentiellement encore en C3-C5, 2) une séparation du mélange de produits obtenu lors de l'étape 1), en trois coupes : une coupe légère contenant les hydrocarbures oléfiniques en C4 et/ou en C5 n'ayant pas réagi, une coupe intermédiaire présentant une T95 comprise entre 200-220°C, et une coupe lourde comprenant le complément, la T95 étant la température à laquelle 95% en poids de produit est évaporé, telle que déterminée selon la méthode normalisée ASTM D2887 ; 3) une oligomérisation de la coupe intermédiaire obtenue à l'étape de séparation, caractérisé par le fait que dans l'étape 3) l'oligomérisation est réalisée en présence d'une coupe d'hydrocarbures oléfiniques en C4 et/ou en C5.

Two stage isomerization process for the production of paraxylene and orthoxylene from a mixture of xylene isomers and ethylbenzene using an activated group VIII catalyst

Procédé d'isomérisation d'une charge contenant des composés aromatiques à huit atomes de carbone caractérisé en ce qu'il comprend au moins une étape a) d'isomérisation effectuée en présence d'un catalyseur contenant au moins un métal du groupe VIII et activé selon un procédé d'activation comprenant au moins une étape de sulfuration et au moins une étape de passivation à l'ammoniac, et au moins une étape b) de déshydrogénation.

PROCESS OF PRODUCTION Of ETHER AND OLEFIN FROM HYDROCARBON CUT CONTAINING AT LEAST a TERTIARY OLEFIN BY SYNTHESIS THEN ETHER DECOMPOSITION COMPRISING a FIRST STAGE OF OLEFIN PURIFICATION BY FRACTIONATION

Procédé de production d'éther et d'oléfine, à partir de coupe hydrocarbonée contenant au moins une oléfine tertiaire, par synthèse d'au moins un éther alkylique tertiaire puis fractionnement pour récupérer une fraction organique contenant de l'éther que l'on décompose en un produit (P1) contenant au moins un alcool et au moins une oléfine tertiaire, qui est fractionné, puis l'on purifie l'oléfine tertiaire dans une zone d'extraction (L1) par lavage à l'eau à partir de laquelle on récupère une fraction contenant l'oléfine tertiaire qui est envoyée dans une zone de séparation (Co) à partir de laquelle on récupère une fraction liquide aqueuse et une fraction liquide hydrocarbonée contenant la majeure partie de l'oléfine tertiaire.

Two-step process for desulphurizing olefinic gasolines comprising arsenic

The invention concerns a fixed bed process for capturing arsenic and for desulphurizing a hydrocarbon fraction comprising olefins, sulphur and arsenic, said process comprising a step a) for bringing a capture mass into contact with said hydrocarbon fraction in the presence of hydrogen, the ratio between the flow rate of hydrogen and the flow rate of the hydrocarbon fraction being in the range 50 to 800 Nm3/m3, the operating temperature being in the range 200° C. to 400° C., the operating pressure being in the range 0.2 to 5 MPa. The capture mass comprises molybdenum in a sulphurized form, nickel in a sulphurized form and at least one porous support selected from the group constituted by aluminas, silica, silica-aluminas, titanium oxide and magnesium oxide. The nickel content is in the range 10% to 28% by weight and the molybdenum content is in the range 0.3% to 2.1% by weight.

PROCEDURE AND DEVICE FOR THE PROCESSING OF A BUTADIENHALTIGEN MATERIAL USED

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND N-PROPANOL

La présente invention concerne un procédé de production d'un mélange d'éthylène et de propylène à partir d'un mélange contenant de l'ethanol, du n-propanol et ayant une teneur en eau comprise entre 30 et 75% poids par rapport au poids total du mélange, dans lequel: a) on met en contact dans une unité de déshydratation le mélange avec un catalyseur de déshydratation choisi parmi: une alumine (A) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 200 et 350 m2/g, un diamètre moyen mésoporeux compris entre 5 et 15 nm, une teneur en sodium inférieure à 50 ppm poids et une teneur en soufre inférieure à 40 ppm poids; et une alumine (B) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 130 et 180 m2/g, un diamètre moyen mésoporeux compris entre 14 et 20 nm, une teneur en sodium comprise entre 300 et 600 ppm poids et une teneur en soufre comprise entre 800 et 1300 ppm poids; la mise en contact étant effectuée à une température ...

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND N-PROPANOL

La présente invention concerne un procédé de production d'un mélange d'éthylène et de propylène à partir d'un mélange contenant de l'ethanol, du n-propanol et ayant une teneur en eau comprise entre 30 et 75% poids par rapport au poids total du mélange, dans lequel: a) on met en contact dans une unité de déshydratation le mélange avec un catalyseur de déshydratation choisi parmi: une alumine (A) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 200 et 350 m2/g, un diamètre moyen mésoporeux compris entre 5 et 15 nm, une teneur en sodium inférieure à 50 ppm poids et une teneur en soufre inférieure à 40 ppm poids; et une alumine (B) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 130 et 180 m2/g, un diamètre moyen mésoporeux compris entre 14 et 20 nm, une teneur en sodium comprise entre 300 et 600 ppm poids et une teneur en soufre comprise entre 800 et 1300 ppm poids; la mise en contact étant effectuée à une température ...

LOW-ENERGY CONSUMPTION METHOD FOR DEHYDRATING ETHANOL INTO ETHYLENE

L'invention décrit un procédé de déshydratation d'une charge éthanol en éthylène comprenant la vaporisation de ladite charge éthanol en mélange avec au moins une partie du flux d'eau purifié recyclé selon l'étape f) dans un échangeur grâce à un échange de chaleur avec l'effluent issu du dernier réacteur, ledit mélange étant introduit dans ladite étape de vaporisation à une pression comprise entre 0,1 et 0,4 MPa, la compression du mélange vaporisé dans un compresseur, l'introduction du mélange vaporisée et comprimée, à une température d'entrée comprise entre 350 et 500°C et à une pression d'entrée comprise entre 0,2 et 1,3 MPa, dans au moins un réacteur adiabatique contenant au moins un catalyseur de déshydratation et dans lequel la réaction de déshydratation a lieu, la séparation de l'effluent issu du dernier réacteur adiabatique de l'étape c) en un effluent comprenant de l'éthylène à une pression inférieure à 1 MPa et un effluent comprenant de l'eau, la purification d'au moins une partie ...

PROCESS OF TREATMENT Of an INTERMEDIATE FRACTION RESULTING From EFFLUENTS DEVAPOCRAQUAGE

Procédé de traitement d'effluents de vapocraquage, comprenant: - la séparation d'une fraction intermédiaire comprenant de l'essence, - un hydrotraitement de cette fraction intermédiaire dans une unité HD1, - un fractionnement de l'effluent de HD1, pour produire une coupe C5 et une coupe C6+, - un fractionnement de la coupe C6+, pour produire une coupe C6-C8 et une coupe C9+, - un hydrotraitement de la coupe C6-C8, - un hydrotraitement de la coupe C9+ pour saturer au moins 20% des aromatiques avec de l'hydrogène excédentaire, et obtenir un solvant, ou une coupe kérosène, ou gazole, ou fuel domestique.

PROCESS FOR the HYDROGENATION OF CUTS CONTAINING OF HYDROCARBONS AND IN PARTICULAR UNSATURATED MOLECULES CONTAINING AT LEAST TWO DOUBLE CONNECTIONS OR AT LEAST TRIPLE CONNECTION

Hydrogénation d'une coupe liquide contenant des hydrocarbures et notamment des molécules insaturées contenant au moins deux doubles liaisons ou au moins une triple liaison dans lequel les molécules insaturées sont au moins partiellement hydrogénées en molécules moins insaturées contenant au moins une double liaison, dans au moins un réacteur comprenant au moins deux lits distincts d'au moins un catalyseur d'hydrogénation, et dans lequel une phase gazeuse contenant de l'hydrogène est introduite pour partie en mélange avec ladite coupe avant le premier lit de catalyseur et pour partie avant les lits suivants contenus dans ledit réacteur.

DEVICE OF DISTRIBUTION MAKING IT POSSIBLE TO CARRY OUT A POLYPHASE MIXTURE ETREACTEUR ASSOCIATES

PROCESS OF PURIFICATION Of an OLEFINIC CUT

Verfahren zur Herstellung von tertiären Olefinen durch Spaltung von tertiären Alkylethern in dem die erste Reinigungsstufe eine Wäsche mit Wasser ist

Verfahren zur Hydrierung von Kohlenwasserstoffschnitten

Abwechselndes Verfahren zur Metathese von Olefinen

Abwechselndes Verfahren zur Metathese von Olefinen

Process for isomerising aromatic compounds containing eight carbon atoms compri sing a recycle

PROCESS FOR DEHYDRATION AND ISOMERIZATION OF C4 ALCOHOLS USING AN AMORPHOUS SOLID WITH SUITABLE POROSITY

La présente invention a pour objet un procédé de production d'oléfines en C4, à partir d'une charge de monoalcool en C4 dans lequel on réalise une réaction de déshydratation du monoalcool en au moins une oléfine, et une réaction d'isomérisation squelettale d'au moins une des oléfines produites dans une même enceinte réactionnelle, en présence d'un catalyseur à base d'alumine à porosité adaptée.

METHOD OF PREPARATION Of a DIESEL CUT BY OLIGOMERIZATION

A new process for the isomerization of eight carbon aromatic compounds to produce para-and ortho-xylenes

Procédé d'isomérisation des composés aromatiques à huit atomes de carbone en présence d'hydrogène dans lequel on ajoute à la charge avant son introduction dans le réacteur d'isomérisation R par la ligne 1 un mélange contenant des composés dont le point d'ébullition est d'environ 80 à 135°C comprenant au moins une paraffine à huit atomes de carbone, au moins un naphtène à huit atomes de carbone, au moins du benzène et au moins du toluène. Ces ajouts sont effectués par un recyclage assuré par la ligne 6 ou par l'addition de composés frais par la ligne 11 ou encore par une combinaison de composés frais et recyclés assurée par ces deux lignes 6 et 11. Un appoint d'hydrogène est assuré par la ligne 15.

PROCESS OF PRODUCTION Of ALPHA OLEFIN, TERTIARY OLEFIN AND/OR ETHER FROM UNSATURATED HYDROCARBON CUT

Procédé de production d'alpha oléfine, d'oléfine tertiaire ou d'éther alkylique tertiaire à partir de coupe hydrocarbonée insaturée contenant au moins une alpha oléfine et au moins une oléfine tertiaire éthérifiable comprenant la synthèse d'au moins un éther alkylique tertiaire pour l'obtention d'un produit qui est séparé en une fraction (O1) appauvrie en éther et contenant ladite alpha oléfine et en une fraction (E1) enrichie en éther, suivie de la décomposition d'au moins une partie de l'éther de la fraction (E1) en un produit (P1) contenant au moins un alcool et au moins une oléfine tertiaire, qui est fractionnée dans une zone de fractionnement (C5) en une fraction (B1) contenant la majeure partie de l'oléfine tertiaire et en une fraction (A1) contenant la majeure partie de l'alcool.

DEVICE OF MIXTURE AND DISTRIBUTION Of a DENSE FLUID AND a LIGHT FLUID PLACES UPSTREAM GRANULAR BED AND ITS USE IN DOWNWARD FLOW

Dispositif de mélange et de répartition d'un fluide dense, généralement liquide, et d'un fluide léger, généralement gazeux, placé dans une enceinte réactionnelle en amont d'un lit (70) granulaire ou entre deux lits granulaires successifs, le dit dispositif étant caractérisé par un système tubulaire (50) d'amenée du fluide dense depuis l'extérieur du réacteur, jusqu'à un niveau inférieur au niveau d'établissement de l'interface entre le fluide dense et le fluide léger, situé au dessus du plateau et de préférence sensiblement voisin de celui du plateau (62). Application de ce dispositif à tout type de réaction gaz/liquide en lit fixe en particulier d'hydrotraitement.

DEVICE IMPROVES OF MIXTURE AND DISTRIBUTION Of a PHASE GAS AND a LIQUID PHASE FEEDING a GRANULAR BED

La présente invention a pour but un dispositif amélioré de mélange et de distribution d'une phase gaz et d'une phase liquide sur un lit granulaire décrit dans une demande précédente. L'amélioration consiste essentiellement en la mise en oeuvre d'une zone annulaire périphérique interne au réacteur par laquelle se fait l'introduction du liquide et qui joue notamment le rôle de zone tampon vis à vis des fluctuations de débit de la phase liquide. L'invention concerne également un réacteur chimique à lit catalytique utilisant un tel dispositif et un procédé de conversion chimique, et notamment d'hydrotraitement d'hydrocarbures utilisant un tel réacteur.

Purification of a 3 carbon olefinic fraction, useful in petrochemical process, comprises isomerizing propadiene to methyl acetylene on a catalyst and selectively hydrogenating the undesirable compounds on a catalyst

Procédé de purification d'une coupe C3 oléfinique comprenant, outre du propylène, des composés indésirables : propadiène (PD) et méthylacétylène (MA), ce procédé comprenant au moins une étape (a) d'isomérisation du PD en MA sur un catalyseur comprenant au moins un élément Eis actif pour l'isomérisation du PD en MA, et au moins une étape (b) d'hydrogénation sélective de ces impuretés pour les convertir en propylène sur un catalyseur comprenant au moins un élément Ehy actif pour l'hydrogénation sélective, l'étape (a) étant préliminaire à l'étape (b) ou réalisée simultanément avec cette étape.

WHEEL FOR VEHICLES

La présente a pour objet un procédé discontinu de fabrication de savon comprenant au moins les étapes suivantes : a. une étape d'empâtage/ cuisson dans laquelle : - on mélange au moins un acide gras et/ou ester d'acide gras avec une solution aqueuse de soude, - on chauffe le mélange pour obtenir une pâte de savon, b. au moins une étape de relargage/lavage de la pâte de savon obtenue à l'étape a. dans laquelle : - la pâte de savon est mélangée avec une solution aqueuse comprenant 1 à 42% en poids d'un mélange de soude et de sel, - le mélange est chauffé, et laissé à décanter jusqu'à formation de deux phases : le savon grainé comprenant du sel, de la soude et de la glycérine, et une solution aqueuse comprenant du sel, de la soude et de la glycérine, le savon grainé et la solution aqueuse sont séparés, c. une étape de lissage du savon grainé obtenu à l'étape b. par neutralisation dans laquelle : - le savon grainé est mélangé avec au moins un agent de neutralisation pouvant être un acide, un ...

CATALYST COMPOSITION COMPRISING MODIFIED CRYSTALLINE ALUMINOSILICATE FOR DEHYDRATION OF ALCOHOLS

Verfahren zur Herstellung von alpha-Olefinen, tertiären Olefinen und/oder Ethern aus einer ungesättigten Kohlenwasserstofffraktion

METHOD FOR JOINTLY PRODUCING PROPYLENE AND PETROL FROM A RELATIVELY HEAVY CHARGE

LOW-ENERGY CONSUMPTION METHOD FOR DEHYDRATING ETHANOL INTO ETHYLENE

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène comprenant: a) Une étape de préchauffe de ladite charge éthanol par échange de chaleur avec l'effluent issu de l'étape e), b) Une étape de prétraitement de la charge éthanol de manière à produire une charge éthanol prétraitée, c) Une étape de vaporisation d'une charge de vaporisation comprenant ladite charge éthanol prétraitée et au moins une partie du flux d'eau traitée recyclée selon l'étape h) dans un échangeur de manière à produire une charge vaporisée, d) Une étape de compression de ladite charge vaporisée de manière à produire une charge comprimée, e) Une étape de déshydratation de ladite charge comprimée dans au moins un réacteur adiabatique, f) Une étape de séparation de l'effluent issu du dernier réacteur adiabatique de l'étape e) en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau. g) Une étape de purification d'au moins une partie de l'effluent comprenant de l'eau issu de ...

Method for direct conversion of a feedstock comprising olefins with four and/or five carbon atoms, for producing propylene with co-production of gasoline

PROCESS FOR the HYDROGENATION OF CUTS CONTAINING OF HYDROCARBONS ETNOTAMMENT OF the UNSATURATED MOLECULES CONTAINING AT LEAST TWO DOUBLE CONNECTIONS OUAU MINUS TRIPLE CONNECTION

DEVICE OF MIXTURE AND DISTRIBUTION Of a DENSE FLUID AND a FLUID LEGERPLACE UPSTREAM OF a GRANULAR BED AND ITS USE IN DOWNWARD FLOW

PROCESS OF JOINT PRODUCTION OF PROPYLENE AND GASOLINE STARTING FROM RELATIVELY HEAVY UNECHARGE

PROCESS OF DESULPHURIZATION Of an EFFLUENT OF CRACKING, OR STEEMCRAQUAGE OR COKING

Desulfurization of charge containing thiophene or thiophenic components

La présente invention concerne un enchaînement d'étapes destinées à désulfurer une essence par exemple de craquage catalytique comportant l'élimination des composés thiophéniques par alkylation de ces composés. Ce procédé particulier permet de ne pas procéder à l'étape d'élimination des composés azotés présents dans les essences à alkyler.

Desulfurization of charge containing thiophene or thiophenic components

La présente invention concerne un enchaînement d'étapes destinées à désulfurer une essence par exemple de craquage catalytique comportant l'élimination des composés thiophéniques par alkylation de ces composés. Une élimination de composés azotés est effectuée en amont de l'étape d'alkylation.

PROCESS OF TERTIARY PRODUCTION Of OLEFIN BY DECOMPOSITION Of ALKYLIC ETHER TERTIARY COMPRISING a FIRST STAGE OF PURIFICATION PER WASHING WITH WATER

Procédé de production d'oléfine tertiaire par décomposition d'éther comprenant a) la décomposition d'un éther en un produit contenant un alcool et une oléfine tertiaire, b) la purification d'au moins une partie du produit issu de a) , dans une zone d'extraction (L1) par lavage à l'eau, pour obtenir une fraction aqueuse (A1) contenant la majeure partie de l'alcool et une fraction (B1) contenant la majeure partie de l'oléfine tertiaire, ladite fraction (B1) contenant ladite oléfine tertiaire, de l'eau, éventuellement de l'éther et des composés légers et étant sensiblement exempte d'alcool, et c) dans laquelle au moins une partie de la fraction (B1) issue de b) est envoyée dans une zone de séparation (Col) à partir de laquelle on récupère une fraction liquide aqueuse (La1) et une fraction liquide (Lb1) contenant la majeure partie de l'oléfine tertiaire et éventuellement de l'éther et éventuellement des composés légers.

PROCESS FOR THE RECOVERY OF ALCOHOLS IN A FERMENTER

La présente concerne un procédé de récupération de produits fermentaires présents dans un moût de fermentation produit dans un bioréacteur (9), comprenant une étape a) dans laquelle on envoie dans le moût de fermentation un flux gazeux (15) sous pression de manière à entrainer au moins une partie des produits et produire un flux gazeux (16) enrichi en produits fermentaires. Le procédé comprend une étape b) de stockage des gaz de fermentation et le flux gazeux qui est envoyé à l'étape a) est constitué par les gaz de fermentation stockés.

PROCEEDED OF HYDROCARBON TRANSFORMATION INTO a FRACTION PRESENTING OCTANE UNINDICE IMPROVES AND a FRACTION HAS STRONG CETANE INDEX

DEVICE Of INJECTION Of a FLUID PLACES BETWEEN TWO SUCCESSIVE LIT MAKING IT POSSIBLE TO CARRY out AND DISTRIBUTE SIMULTANEOUSLY a POLYPHASE MIXTURE

Dispositif d'injection d'un fluide secondaire placé entre deux lits granulaires successifs permettant de réaliser et de distribuer un mélange polyphasique entre ledit fluide secondaire et un fluide ou un mélange de fluides issu du lit granulaire supérieur, comportant une chambre d'injection du fluide secondaire, l'injection du fluide secondaire étant effectuée au niveau dudit dispositif, et des moyens permettant la mise en contact dudit fluide secondaire et d'au moins une partie du fluide ou du mélange de fluides issu du lit granulaire supérieur et la distribution simultanée du mélange résultant de ladite mise en contact vers le lit granulaire inférieur.

PROCESS Of IMPROVEMENT OF CUTS GASOLINES AND TRANSFORMATION INTO GAZOLES

L'invention concerne un procédé de transformation d'une charge d'hydrocarbures comprenant des oléfines linéaires et ramifiées comprenant les étapes suivantes: a) une étape de séparation par membrane de la charge hydrocarbonée dans des conditions permettant de produire une coupe β contenant la majorité des oléfines linéaires présentes dans ladite charge, et une coupe γ contenant la majorité des oléfines ramifiées, b) une étape de traitement des oléfines linéaires contenues dans les effluents issus de l'étape de séparation sur membrane ( coupe β) dans des conditions d'oligomérisation modérées, c) une étape de séparation par distillation des effluents issus de l'étape d'oligomérisation en au moins deux coupes, d) une étape d' hydrogénation de la coupe η dans des conditions d'obtention d'un gazole à fort indice de cétane.

Desulfurization of charge containing thiophene or thiophenic components

La présente invention concerne un enchaînement d'étapes destinées à désulfurer une essence par exemple de craquage catalytique comportant l'élimination des composés thiophéniques par alkylation de ces composés. Ce procédé particulier permet de ne pas procéder à l'étape d'élimination des composés azotés présents dans les essences à alkyler.

Preparing catalyst for olefin transformation comprises preparing oxide colloidal suspension, contacting promoter precursor with colloidal suspension, contacting and drying colloidal suspension with support to give catalyst

Preparation of a catalyst (I) having a metal (Ia) and a promoter (Ib) on a support comprises: preparing an oxide colloidal suspension of (Ia), comprising neutralization of a basic solution with a mineral acid solution that has precursor of (Ia); contacting precursor of (Ib) with the colloidal suspension either directly in crystallized form or after dissolution in aqueous phase; contacting the obtained colloidal suspension with the support; and drying at 30-200[deg]C under an air-flow. An independent claim is included for a process of cracking olefins comprising implementing (I).

THE USE OF A REACTOR IN A PROCESS FOR MAKING SOAP AND REACTOR ESPECIALLY ADAPTED FOR SUCH USE

Utilisation d'un réacteur (1) dans un procédé de fabrication de savon, le réacteur (1) comprenant une cuve (2) comportant un espace intérieur (5) et un système d'agitation (10) déplaçable dans l'espace intérieur (5) de la cuve (2), le procédé de fabrication étant discontinu et comprenant au moins une étape d'empâtage et de cuisson prévoyant de réaliser un mélange d'au moins un corps gras et d'une base dans l'espace intérieur (5) de la cuve (2), et de chauffer le mélange, dans laquelle, au cours de l'étape d'empâtage et de cuisson, le système d'agitation (10) est déplacé dans le mélange de manière à faire circuler le mélange et à cisailler au moins localement le mélange.

Verfahren zur Isomerisierung von C8-Aromaten unter Verwendung einer Recyclierung

Method for producing middle distillates by hydroisomerisation and hydrocracking of a heavy fraction from a Fischer-Tropsch effluent

METHOD FOR PRODUCING MIDDLE DISTILLATES BY HYDROISOMERISATION AND HYDROCRACKING OF A HEAVY FRACTION FROM A FISCHER-TROPSCH EFFLUENT

L'invention décrit un procédé dans lequel l'effluent paraffinique issu d'une unité de synthèse Fischer-Tropsch est séparé de façon à obtenir une fraction C5+ lourde, cette fraction lourde étant ensuite hydrogénée en présence d'un catalyseur d'hydrogénation à une température comprise entre 100° C et 180° C, à une pression totale comprise entre 0,5 à 6 MPa, à une vitesse volumique horaire comprise entre 1 et 10h -1, et à un débit d'hydrogène correspondant à un rapport volumique hydrogène /hydrocarbure s compris entre 5 à 80 N1 /1 /h, l'effluent hydrogéné liquide étant ensuite mis en contact avec un catalyseur d'hydroisomérisation/hydrocraquage, sans étape de séparation préable, l'effluent hydroisomérisé/hydrocraqué, sans étape ensuite distillé pour obtenir les distillats moyens et éventuellement des bases huiles.

METHOD FOR PRODUCING MIDDLE DISTILLATES BY HYDROISOMERISATION AND HYDROCRACKING OF A HEAVY FRACTION FROM A FISCHER-TROPSCH EFFLUENT

L'invention décrit un procédé dans lequel l'effluent paraffinique issu d'une unité de synthèse Fischer-Tropsch est séparé de façon à obtenir une fraction C5+ lourde, cette fraction lourde étant ensuite hydrogénée en présence d'un catalyseur d'hydrogénation à une température comprise entre 100° C et 180° C, à une pression totale comprise entre 0,5 à 6 MPa, à une vitesse volumique horaire comprise entre 1 et 10h -1, et à un débit d'hydrogène correspondant à un rapport volumique hydrogène /hydrocarbure s compris entre 5 à 80 N1 /1 /h, l'effluent hydrogéné liquide étant ensuite mis en contact avec un catalyseur d'hydroisomérisation/hydrocraquage, sans étape de séparation préable, l'effluent hydroisomérisé/hydrocraqué, sans étape ensuite distillé pour obtenir les distillats moyens et éventuellement des bases huiles.

METHOD FOR PRODUCING ETHYLENE OXIDE FROM A THERMALLY INTEGRATED ETHANOL STREAM

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène puis d'oxydation de l'éthylène en oxyde d'éthylène comprenant une étape de vaporisation d'une charge comprenant ladite charge éthanol et au moins une partie d'un flux d'eau de dilution comprenant de l'éthanol recyclé de manière à produire une charge vaporisée, une étape de déshydratation d'un mélange comprenant ladite charge vaporisée et un flux vaporisé d'eau de dilution comprenant de l'éthanol, une étape de séparation de l'effluent issu de l'étape de déshydratation en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau, une étape de purification d'au moins une partie de l'effluent comprenant de l'eau et la séparation en au moins un flux d'eau traitée et un flux d'eau de dilution comprenant de l'éthanol, une étape de recyclage et de vaporisation d'au moins une partie du flux d'eau de dilution comprenant de l'éthanol issu de l'étape de séparation par vaporisation partielle ou totale dans ...

LOW-ENERGY CONSUMPTION METHOD FOR DEHYDRATING ETHANOL INTO ETHYLENE

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène comprenant: a) Une étape de préchauffe de ladite charge éthanol par échange de chaleur avec l'effluent issu de l'étape e), b) Une étape de prétraitement de la charge éthanol de manière à produire une charge éthanol prétraitée, c) Une étape de vaporisation d'une charge de vaporisation comprenant ladite charge éthanol prétraitée et au moins une partie du flux d'eau traitée recyclée selon l'étape h) dans un échangeur de manière à produire une charge vaporisée, d) Une étape de compression de ladite charge vaporisée de manière à produire une charge comprimée, e) Une étape de déshydratation de ladite charge comprimée dans au moins un réacteur adiabatique, f) Une étape de séparation de l'effluent issu du dernier réacteur adiabatique de l'étape e) en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau. g) Une étape de purification d'au moins une partie de l'effluent comprenant de l'eau issu de ...

PROCESS FOR THE OLIGOMERIZATION OF OLEFINS USING A CATALYST BASED ON SILICA-ALUMINA.

On décrit un procédé d'oligomérisation d'une charge hydrocarbonée oléfinique consistant en la mise en contact de ladite charge avec un catalyseur comprenant une silice - alumine, la teneur massique en silice dudit catalyseur étant comprise entre 5 et 95% poids, ledit catalyseur étant préparé selon un procédé comprenant au moins :a) le mélange d'au moins un composé aluminique partiellement soluble en milieu acide avec soit au moins un composé silicique totalement soluble dans le mélange réactionnel soit une combinaison formée d'au moins un composé silicique et d'au moins un composé aluminique, lesdits composés silicique et aluminique étant totalement solubles dans le mélange réactionnel, de manière à former un solide précurseur dudit catalyseurb) le traitement hydrothermal, pendant une durée d'au moins 3 heures, du solide issu de ladite étape a). A process for the oligomerization of an olefinic hydrocarbon feed is described, consisting in bringing said feed into contact with a catalyst comprising a silica - alumina, the silica content by mass of said catalyst being between 5 and 95% by weight, said catalyst being prepared according to a process comprising at least: a) the mixture of at least one aluminum compound partially soluble in acidic medium with either at least one silicic compound completely soluble in the reaction mixture or a combination formed of at least one silicic compound and d 'at least one aluminum compound, said silica and aluminum compounds being completely soluble in the reaction mixture, so as to form a solid precursor of said catalyst b) hydrothermal treatment, for a period of at least 3 hours, of the solid resulting from said step To).

Process for joint production of propylene and catalytic cracking of mixture of heavy and light hydrocarbon charges, the light charge comprising oligomers formed from C4/5 olefins

Conversion of a charge comprising a main heavy fraction of boiling point more than 350degreesC and a secondary fraction of boiling point less than 320degreesC by catalytic cracking in a fluidized bed, to obtain good yields of both propylene and petrol. Process for conversion of a charge made up of a main heavy hydrocarbon fraction of boiling point more than 350degreesC and a secondary light fraction of which the boiling point less than 320degreesC, in which: (a) The main charge (at least 50% wt. of the total charge) is cracked in a fluidized bed reactor in the presence of a catalyst; (b) The secondary charge is cracked in a fluidized bed with the same catalyst, separately or with the main charge; the secondary charge comprises 8C+ olefins obtained by oligomerization of 4 and/or 5C olefins; and (c) The effluents obtained are fractionated in a common fractionation zone and the catalysts are regenerated in a common regeneration zone.

Upgrading a hydrocarbon feed and lowering its vapor pressure comprises contacting a pentene fraction with a higher olefin fraction in the presence of a dimerization/alkylation catalyst to produce gasoline and kerosene

On décrit un procédé de valorisation d'une charge d'hydrocarbures et de diminution de la tension de vapeur de ladite charge comprenant trois étapes : une étape a) consistant à séparer ladite charge d'hydrocarbures en une fraction (O1) comprenant essentiellement des composés contenant 5 atomes de carbone dont au moins 2% poids de pentènes, une étape b) consistant à mettre en contact ladite fraction (O1) avec une coupe d'hydrocarbures (02) comprenant au moins en partie des hydrocarbures présentant un nombre d'atomes de carbone compris entre 6 et 10, dont au moins 2 % poids d'oléfines, et une étape c) consistant à séparer les effluents issus de l'étape b) en une coupe essence (α) dont le point supérieur de distillation est inférieur à 100°C et une coupe kérosène (β) d'intervalle de distillation compris entre 100°C et 300°C.

PROCEEDED Of ISOMERIZATION OF COMPOSE AROMATIC HAS EIGHT CARBON ATOMS ENDEUX SUCCESSIVE STAGES

METHOD FOR PRODUCING PROPYLENE IN THE PRESENCE OF A MACROPOROUS CATALYST IN THE FORM OF SPHERICAL BALLS

On décrit un procédé de conversion directe d'une charge hydrocarbonée comprenant au moins des oléfines ayant 4 atomes de carbone et au moins des oléfines ayant 5 atomes de carbone pour la production de propylène, ledit procédé comprenant le passage de ladite charge dans au moins une unité réactionnelle pourvue d'au moins un catalyseur se présentant sous forme de billes sphériques de diamètre compris entre 1 et 3 mm, chacune desdites billes sphériques comprenant au moins une zéolithe et au moins un support à base d'alumine et présentant une distribution poreuse telle que le volume macroporeux mesuré par porosimétrie au mercure est compris entre 0,10 et 0,20 ml/g et le volume mésoporeux mesuré par porosimétrie au mercure est compris entre 0,25 et 0,35 ml/g.

THE USE OF A REACTOR IN A PROCESS FOR MAKING SOAP AND REACTOR ESPECIALLY ADAPTED FOR SUCH USE

Utilisation d'un réacteur (1) dans un procédé de fabrication de savon, le réacteur (1) comprenant une cuve (2) comportant un espace intérieur (5) et un système d'agitation (10) déplaçable dans l'espace intérieur (5) de la cuve (2), le procédé de fabrication étant discontinu et comprenant au moins une étape d'empâtage et de cuisson prévoyant de réaliser un mélange d'au moins un corps gras et d'une base dans l'espace intérieur (5) de la cuve (2), et de chauffer le mélange, dans laquelle, au cours de l'étape d'empâtage et de cuisson, le système d'agitation (10) est déplacé dans le mélange de manière à faire circuler le mélange et à cisailler au moins localement le mélange.

Device for separate injection and homogeneous distribution of two fluids

A device that is placed in a vessel for carrying out separate injection ( 1,6 ) of two fluids in two different physical states, or which are not miscible, and for homogeneous distribution of at least one of the two fluids in the vessel downstream of said device. The first fluid is injected (6) into the vessel at least one point level with said device, said device being characterized in that it contains a chamber ( 5 ) pierced by orifices ( 7, 8 ) for the passage of a first fluid. Said chamber ( 5 ) is also imperviously traversed by tubes ( 4 ) or conduits with a free end acting as a passage through said chamber for the second fluid.

Verfahren zur Aufbereitung einer Zwischenfraktion von Dampfspaltungsströmen

Verfahren zur Herstellung von tertiären Olefinen durch Spaltung von tertiären Alkylethern

METHOD FOR SIMULTANEOUSLY ELIMINATING ISOBUTANAL AND ACETONE FROM OLEFINIC FEEDSTOCKS BY ADSORPTION ON A ZEOLITE MATERIAL

La présente invention concerne un procédé de purification d'une charge oléfinique comprenant des oléfines à 4 atomes de carbone et des impuretés incluant l'isobutanal, l'éthanol et l'acétone, ledit procédé comprenant un pré-traitement comprenant au moins une étape d'élimination de l'éthanol et de l'eau présents dans ladite charge oléfinique et une étape d'élimination simultanée de l'isobutanal et de l'acétone, par passage de la charge issue du pré-traitement sur au moins un lit fixe d'au moins un adsorbant comprenant au moins un matériau à charpente zéolithique, ledit matériau à charpente zéolithique étant choisi dans le groupe constitué par : les zéolithes, AlPOs, SAPOs et leurs mélanges; ladite étape d'élimination simultanée de l'isobutanal et de l'acétone opérant à une température entre 0 et 200°C, à une pression de 0,1 à 10 MPa et avec une vitesse volumique horaire (VVH) de la charge sur le lit fixe compris entre 0,1 et 10 h-1.

Process for producing middle distillates by hydroisomerization and hydrocracking of a heavy fraction derived from a fischer-tropsch effluent

The present invention describes a process for producing middle distillates from a C5+ liquid paraffinic fraction, termed a heavy fraction, with an initial boiling point in the range 15° C. to 40° C. produced by Fischer-Tropsch synthesis, comprising the following steps in succession: passing said C5+ liquid paraffinic fraction, termed a heavy fraction, over at least one ion exchange resin at a temperature in the range 80° C. to 150° C., at a total pressure in the range 0.7 to 2.5 MPa, at an hourly space velocity in the range 0.2 to 2.5 h −1 ; eliminating at least a portion of the water formed in step a); hydrogenating the unsaturated olefinic type compounds of at least a portion of the effluent derived from step b) in the presence of hydrogen and a hydrogenation catalyst; and hydroisomerization/hydrocracking of at least a portion of the hydrotreated effluent derived from step c) in the presence of hydrogen and a hydroisomerization/hydrocracking catalyst.

PROCESS FOR DEHYDRATION OF DILUTE ETHANOL INTO ETHYLENE WITH LOW ENERGY CONSUMPTION WITHOUT RECYCLING OF WATER

A process for dehydration of an ethanol feedstock into ethylene, comprising the vaporization of said dilute hydrated ethanol feedstock in an exchanger, with heat exchange with the effluent that is obtained from a last reactor, with said mixture being introduced into said vaporization stage at a pressure that is lower than the pressure of the effluent that is obtained from the last reactor, the compression of the mixture that is vaporized in a compressor, the introduction of the vaporized and compressed mixture, into at least one adiabatic reactor that contains at least one dehydration catalyst. 1. Process for dehydration of an ethanol feedstock , which comprises a percent by mass of ethanol of between 2 and 55% by weight , into ethylene comprising:a) The vaporization of said dilute ethanol feedstock in an exchanger, owing to an exchange of heat with the effluent that is obtained from the last reactor, said ethanol feedstock being introduced into said vaporization stage at a pressure that is lower than the pressure of the effluent that is obtained from the last reactor,b) The compression of said feedstock that is vaporized in a compressor,c) The introduction of said vaporized and compressed feedstock, at an entrance temperature of between 350 and 550° C. and at an entrance pressure of between 0.3 and 1.8 MPa, in at least one adiabatic reactor that contains at least one dehydration catalyst and in which the dehydration reaction takes place,d) The separation of the effluent that is obtained from the last adiabatic reactor of stage c) into an effluent that comprises ethylene at a pressure that is lower than 1.6 MPa and an effluent that comprises water,e) The purification of at least a portion of the effluent that comprises water that is obtained from stage d) and the separation of at least one stream of unconverted ethanol, with no recycling of said stream of purified water that is obtained from said stage e) being done upstream from stage a).2. Process according to ...

PROCESS FOR DEHYDRATION AND ISOMERIZATION OF C4 ALCOHOLS USING AN AMORPHOUS SOLID WITH SUITABLE POROSITY

The present invention relates to a method of producing C4 olefins, from a feed of C4 monohydric alcohol, in which a reaction of dehydration of the monohydric alcohol to at least one olefin, and a reaction of skeletal isomerization of at least one of the olefins produced in one and the same reaction vessel, are carried out in the presence of an alumina-based catalyst with adapted porosity. 1. Method of producing C4 olefins , by passing a feed of C4 monohydric alcohol over a catalyst , in which a reaction of dehydration of the monohydric alcohol to at least one olefin , and a reaction of skeletal isomerization of at least one of the olefins produced in one and the same reaction vessel , are carried out , said method being characterized in that the reactions of dehydration and of isomerization are carried out in the presence of the catalyst , optionally containing a promoter , said catalyst being based on alumina , free from halogens and having a pore distribution such that the volume of pores with diameter greater than 0.1 μm measured by mercury porosimetry according to standard ASTM D4284-83 is comprised between 10 mL/100 g and 30 mL/100 g.2. Method according to claim 1 , in which the catalyst comprises at least 50 wt. % of gamma alumina.3. Method according to claim 1 , in which said catalyst is in the form of spheroids claim 1 , preferably having an average diameter comprised between 1 and 2.5 mm.4. Method according to claim 1 , in which said catalyst has a surface area Scomprised between 180 and 270 m/g.5. Method according to claim 1 , in which said catalyst has a total pore volume defined by analysis using mercury porosimetry comprised between 0.45 and 0.9 ml/g6. Method according to claim 1 , in which a promoter selected from the group comprising metals of groups 4 claim 1 , 5 claim 1 , 6 and/or 12 is added to said catalyst.7. Method according to claim 6 , in which the promoter is selected from the group comprising Ti claim 6 , V claim 6 , W.8. Method according to ...

Process for dehydration of ethanol into ethylene with low energy consumption

A process for dehydration of an ethanol feedstock into ethylene, comprising the vaporization of said ethanol feedstock in a mixture with at least a portion of the recycled purified water stream from heat exchange with the effluent that is obtained from the last reactor.

METHOD AND PROCESS FOR CONVERTING THE ETHYLENE PRESENT IN THE OVERHEAD EFFLUENT FROM A FCC IN A MANNER SUCH AS TO INCREASE THE PROPYLENE PRODUCTION

The present invention describes a process for fractionating the gaseous fraction leaving overhead from the fractionation column of a catalytic cracking unit (FCC) using a unit for the conversion of ethylene into propylene, in order to upgrade the ethylene contained in the fuel gas. 1. A device for fractionating the gaseous fraction leaving the head of the fractionation column of a catalytic cracking unit , the fraction containing LPG , light gasoline , and a residual gas termed “fuel gas” which itself contains a certain quantity of ethylene , the device comprising:{'b': 6', '15', '10, 'a first absorption section () which can be used to separate the fuel gas () and the light gasoline and LPG stream (), said section being present in an existing catalytic cracking unit,'}{'b': 22', '15, 'a unit () for the catalytic conversion of ethylene into propylene and other products of interest, wherein the feed is constituted by the fuel gas (), in which a large portion of the ethylene is essentially converted into propylene and also into aromatics and other products of interest, in the presence of a catalyst based on zeolite,'}{'b': 31', '22', '31', '11, 'a novel absorption section () which admits the effluents from the conversion unit () after recompression, the propylene, butene and the gasoline fractions contained in said effluents being recovered in said novel absorption section (), by using the gasoline arriving from the existing debutanizer (),'}{'b': 16', '33', '31, 'a second absorption section (), which admits the gas () obtained from the novel absorption section (),'}{'b': 35', '34', '31', '36', '37, 'a debutanization section () which admits the LPG and gasoline fractions () obtained from the novel absorption section () and which produces a stabilized gasoline () and a light LPG fraction ().'}222223227224223227225227228. The device for fractionating the gaseous fraction leaving the head of the fractionation column of a catalytic cracking unit as claimed in claim 1 , in ...

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND ISOPROPANOL

Production of a mixture of ethylene and propylene from a mixture containing ethanol and isopropanol and having a water content between 30 and 75 wt. % is obtained by a process comprising: 2. Process according to claim 1 , in which the mixture contains between 1 and 75% by weight of ethanol and between 99 and 25% by weight of isopropanol with respect to the total weight of ethanol and isopropanol.3. Process according to claim 1 , in which the aluminas (A) and (B) are gamma aluminas.4. Process according to claim 1 , in which the alumina (A) has a mean mesopore diameter comprised between 6 and 12 nm and preferably comprised between 7 and 11 nm.5. Process according to claim 1 , in which the alumina (B) has a BET specific surface area measured according to the standard ASTM D 3663-03 comprised between 150 and 180 m/g.6. Process according to claim 1 , in which the alumina (B) has a mean mesopore diameter comprised between 15 and 20 nm.7. Process according to claim 1 , in which when the mixture also comprises butanol claim 1 , said mixture is treated in order to separate the butanol before dehydration stage a).8. Process according to claim 7 , in which a separation of the butanol is carried out by distillation.930305343735. Process according to claim 1 , in which before stage a) the mixture is brought into contact with an aromatic cut comprising a mixture of aromatic compounds having 7 to 10 carbon atoms claim 1 , in a separation unit comprising a liquid-liquid extraction column () claim 1 , so as to separate from said extraction column () an aqueous fraction () and an organic fraction containing the aromatic cut claim 1 , ethanol and isopropanol claim 1 , and said organic fraction is sent into a distillation column () configured in order to extract an effluent () containing the aromatic cut and a mixture () containing ethanol and isopropanol claim 1 , and said mixture is sent into the dehydration unit.10. Process according to claim 9 , in which the aromatic cut is a ...

LOW-ENERGY CONSUMPTION METHOD FOR DEHYDRATING ETHANOL INTO ETHYLENE

A process for dehydrating an ethanol feedstock to give ethylene, includes: 1. A process for dehydrating an ethanol feedstock to give ethylene , comprising:a) a stage for vaporizing a vaporization feedstock comprising said ethanol feedstock in an exchanger by means of a heat exchange with a dehydration effluent resulting from stage c), so as to produce a vaporized feedstock;b) a stage for heating said vaporized feedstock in an exchanger by means of a heat exchange with a thermal fluid, so as to produce a superheated feedstock having a temperature of greater than 400° C. and less than 550° C.;c) a stage for dehydrating said superheated feedstock so as to produce a dehydration effluent, wherein said stage for dehydrating comprises a reaction section comprising at least one multitubular reactor in which the dehydration reaction takes place, said multitubular reactor comprising a plurality of tubes having a length of between 2 and 4 m and a shell, said tubes each comprising at least one fixed bed comprising at least one dehydration catalyst, said superheated feedstock being introduced into said tubes at an inlet temperature of greater than 400° C. and less than 550° C. and at an inlet pressure of between 0.8 and 1.8 MPa,a heat transfer fluid circulating inside said shell at a mass flow rate such that the ratio of the mass flow rate of said heat transfer fluid in the shell relative to the mass flow rate of said superheated feedstock introduced into said tubes is greater than or equal to 10, said heat transfer fluid having a temperature at the inlet into the shell of said multitubular reactor of greater than 430° C. and less than 550° C.;d) a stage for separating the dehydration effluent resulting from stage c) into an effluent comprising ethylene at a pressure of less than 1 MPa and an effluent comprising water;e) a stage for purifiying at least a portion of the effluent comprising water resulting from staged) and the separation of at least one stream of purified water ...

METHOD FOR CLEANING A SOLID SUPPORT OF A FERMENTATION REACTOR COMPRISING A CONTAMINATED POLYURETHANE FOAM

The present invention relates to a process for cleaning a solid support of a fermentation reactor for the production of alcohols by fermentation using a sugary fluid, the solid support comprising a polyurethane foam inoculated with a biomass produced by a solvent-producing strain belonging to the genus , the process comprising placing the solid support in contact with a fluid originating from the fermentation must enriched in alcohol and/or acetone and/or an aqueous solution at basic pH. 132Clostridium. A process for cleaning a solid support of a fermentation reactor () for the production of alcohols by fermentation using a sugary fluid () , the solid support comprising a polyurethane foam inoculated with a biomass produced by a solvent-producing strain belonging to the genus , the process comprising placing the solid support in contact with a fluid originating from the fermentation must enriched in alcohol and/or acetone and/or an aqueous solution at basic pH.2. The process as claimed in claim 1 , in which the fluid originating from the fermentation must comprises at least one compound chosen from butanol claim 1 , isopropanol and ethanol.3. The process as claimed in claim 2 , in which the fluid originating from the fermentation must comprises butanol.4. The process as claimed in claim 2 , in which the fluid originating from the fermentation must comprises at least 10 g/L of the compound.51. The process as claimed in claimed claim 2 , in which the fluid originating from the fermentation must comprises at least one element from the group consisting of:{'b': 18', '21', '22', '27', '28, 'a source of butanol, a beer-column head effluent (), a beer-column reflux (), a beer-column distillate (), an isopropanol-ethanol-water column head mixture (), a source of isopropanol, an isopropanol-ethanol-water column tail effluent (), and a source of acetone.'}6. The process as claimed in claim 5 , in which the source of butanol comprises at least 90% by weight of butanol.718. The ...

Selective catalyst for hydrogenolysis of ethyl-aromatics by conserving methyl-aromatics

The present invention relates to a hydrogenolysis process wherein a hydrocarbon-based feedstock comprising aromatic compounds having at least 8 carbon atoms is treated by means of a hydrogen feed and in the presence of a catalyst, in order to convert C2+ alkyl chains of said aromatic compounds into methyl groups and to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds, wherein the catalyst comprises a support, comprising at least one refractory oxide, and an active phase comprising nickel and molybdenum, wherein: the nickel content being between 0.1 and 25% by weight relative to the total weight of the catalyst; the molybdenum content being between 0.1 and 20% by weight relative to the total weight of the catalyst; and the catalyst comprising a molar ratio of molybdenum to nickel of between 0.2 and 0.9. The present invention also relates to said catalyst and to the process for preparing said catalyst.

COUPLING OF UNIT FOR EXTRACTING METHYL-SUBSTITUTED AROMATICS WITH UNIT FOR HYDROGENOLYSING ALKYL-AROMATICS

The present invention relates to a device and a process for converting aromatic compounds, wherein: methyl-substituted aromatic compounds are extracted from a hydrocarbon feedstock () comprising aromatic compounds having at least 8 carbon atoms in an extraction unit (), to produce at least one effluent enriched in methyl-substituted aromatic compounds (A, B) and an effluent depleted in methyl-substituted aromatic compounds (); and C2+ alkyl chains of the aromatic compounds of the depleted effluent () are converted into methyl groups in a hydrogenolysis unit () placed downstream of the extraction unit (), to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds ().

METHOD FOR TREATING AN ALCOHOL FEEDSTOCK FOR THE PRODUCTION OF OLEFINS

The invention relates to a process for treating an alcoholic feedstock, comprising: a) a stage of preheating of said alcoholic feedstock to a temperature of between 70° C. and 200° C.; b) a stage of pretreatment on an acidic solid, operating at a temperature of between 70° C. and 200° C., to produce a pretreated alcoholic feedstock; c) a stage of partial vaporization to produce a vaporized stream and a liquid stream; and d) a stage of purification of the liquid stream resulting from stage c), to give a stream rich in water, a stream rich in monoalcohol and a stream rich in impurities. 1. A process for treating an alcoholic feedstock containing at least one monoalcohol , comprising the following stages:a) a stage of preheating of said alcoholic feedstock to a temperature of between 70° C. and 200° C., to produce a preheated alcoholic feedstock;b) a stage of pretreatment of said preheated alcoholic feedstock on an acidic solid, operating at a temperature of between 70° C. and 200° C., to produce a pretreated alcoholic feedstock;c) a stage of partial vaporization of a vaporization feedstock to produce a gaseous stream and a liquid stream, said vaporization feedstock comprising said pretreated alcoholic feedstock obtained at the end of stage b), said partial vaporization stage comprising a partial vaporization section fed with said vaporization feedstock at an inlet pressure of between 0.1 and 1.4 MPa, to produce said gaseous stream and said liquid stream such that the gaseous stream represents at least 70% by weight of the weight of the vaporization feedstock;d) a stage of purification of the liquid stream resulting from stage c), to give a stream rich in water, a stream rich in monoalcohol and a stream rich in impurities.2. The treatment process as claimed in claim 1 , wherein said alcoholic feedstock is an alcohol feedstock produced from renewable resources derived from biomass claim 1 , preferably by fermentation.3. The treatment process as claimed in claim 1 , ...

METHOD FOR DEHYDRATING AND ISOMERISING ALCOHOLS USING A NON-ZEOLITE ALUMINOSILICATE SOLID

Process for simultaneous dehydration and skeletal isomerization of a feedstock that comprises at least one Cmonoalcohol and that contains between 0.5 and 50% water, for the purpose of producing Calkenes, with said process operating at a temperature of between 250 and 550° C., under a pressure of between 0.1 and 1 MPa, with an hourly volumetric flow rate of between 0.1 and 10 h, characterized in that it uses a catalyst that comprises at least one non-zeolitic aluminosilicate-type solid. 2. Process according to claim 1 , such that said feedstock for the most part comprises isobutanol.3. Process according to claim 1 , such that said silicic compound used in said stage a) is selected from among silicic acid claim 1 , the sols of silicic acid claim 1 , the water-soluble alkaline silicates claim 1 , and the cationic salts of silicon claim 1 , taken by itself or in a mixture.4. Process according to claim 1 , such that said aluminum compound used in said stage a) is selected from among boehmite claim 1 , pseudo-boehmite and the amorphous or essentially amorphous alumina gels claim 1 , taken by itself or in a mixture.5. Process according to claim 1 , such that said aluminosilicate-type solid has a silica content by mass of between 4 and 25% by weight of said solid.6. Process according to claim 5 , such that said aluminosilicate-type solid has a silica content by mass of between 4 and 15% by weight of said solid.7. Process according to claim 1 , such that said aluminosilicate-type solid has a silica content by mass of between 35 and 95% by weight of said solid.8. Process according to claim 7 , such that said aluminosilicate-type solid has a silica content by mass of between 35 and 50% by weight of said solid.9. Process according to claim 1 , such that said aluminosilicate-type solid has a cationic impurities content by mass that is less than 0.1% by weight of the catalyst.10. Process according to claim 1 , such that said aluminosilicate-type solid has an anionic impurities ...

METHOD FOR DEHYDRATING ALCOHOLS TO OBTAIN OLEFINS, INVOLVING A STEP OF CATALYST SELECTIVATION

The invention relates to a process for dehydrating alcohols to olefins, comprising a reaction step and a catalyst selectivation step. 1. A process for dehydrating alcohols to olefins , comprising:{'sup': '−1', 'a) a reaction step fed with a feedstock comprising at least one alcohol, said reaction step being performed in the gas phase at a weighted average temperature of between 250 and 400° C., at a pressure of between 0.2 MPa and 1 MPa and at a WWH of between 1 and 18 hin the presence of a catalyst comprising a zeolite comprising at least one series of channels the opening of which is defined by a ring of 8 oxygen atoms (8 MR) producing an olefin effluent;'}b) a catalyst selectivation step comprising, for a period of between 0.5 and 5 hours, stoppage of the feed and maintenance of the temperature and pressure of said step a);c) resumption of the feed on conclusion of step b) with return to the conditions of step a);said selectivation step being performed when the selectivity toward isoolefins n of said step a) is greater than 25%, or when the conversion into alcohols of said step a) is less than 99%.2. The process as claimed in claim 1 , in which said feedstock comprises from 40% to 100% by weight of at least one alcohol.3. The process as claimed in claim 1 , in which said feedstock comprises at least one primary monoalcohol of formula R—CH—OH claim 1 , in which R is a nonlinear alkyl radical of general formula CHwhere n is an integer between 3 and 20.4. The process as claimed in claim 1 , in which said primary monoalcohol is isobutanol or 2-methyl-1-butanol claim 1 , taken alone or as a mixture.5. The process as claimed in claim 1 , in which said zeolite also contains at least one series of channels claim 1 , the pore opening of which is defined by a ring containing 10 oxygen atoms (10 MR).6. The process as claimed in claim 1 , in which said zeolite is chosen from zeolites of the FER and MFS structural types claim 1 , taken alone or as a mixture.7. The process as ...

METHOD FOR ISOMERISING DEHYDRATION OF A NON-LINEAR PRIMARY MONOALCOHOL ON A QUADRILOBED IRON ZEOLITE CATALYST

A method for isomeris ng dehydration in the presence of a specific catalyst, to produce at least one alkene, carried out on a feedstock containing a non-linear primary monoalcohol, where the catalyst includes a zeolite having a series of 8MR channels and a binder having certain pore volume, which catalyst is multilobe-shaped and has characteristics including certain average mesopore volume Vm, and mesopores having a certain diameter, an average certain macropore volume VM, the macropores having a certain diameter, and certain average micropore volume Vμ, the micropores having a certain diameter, and the catalyst has a certain exposed geometric area. 1. A process for isomerizing dehydration of a feedstock comprising , alone or in a mixture , a primary monoalcohol of formula R—CH—OH , in which R is a nonlinear alkyl radical of general formula CHwhere n is an integer of between 3 and 20 , said process comprising a step of isomerizing dehydration operated in the gas phase at a weighted average temperature of between 250 and 460° C. , at a pressure of between 0.2 MPa and 1 MPa , at a weight hourly space velocity (WWH) of between 1 and 25 h , in the presence of a catalyst comprising at least one zeolite and at least one binder , in which the amount by weight Tz of zeolite is 55-90 wt % relative to the total weight of said catalyst and in which said zeolite has at least one series of channels with an aperture of 8 oxygen atoms (8MR) , said binder having a pore volume of between 0.5 and 0.9 ml/g , the catalyst being multilobate and havingan average mesopore volume Vm centered at plus or minus 20% around the value defined by the formula Vm=−0.004Tz+0.505, the mesopores having a diameter of 3.6 nm to 50 nm,an average macropore volume VM centered at plus or minus 20% around the value defined by the formula VM=0.0101Tz 0.5375, the macropores having a diameter of more than 50 nm and less than 7000 nm,an average micropore volume Vμ centered at plus or minus 20% around the value ...

Modified Crystalline Aluminosilicate for Dehydration of Alcohols

The present invention relates to a catalyst composition comprising a modified crystalline aluminosilicate of the Framework Type FER having Si/Al framework molar/ratio greater than 20 characterized in that in said modified crystalline aluminosilicate the ratio between the strong acid sites and the weak acid sites, S/W, is lower than 1.0 and having the extra framework aluminum (EFAL) content lowered to less than 10 wt % preferably 5 wt % even more preferably less than 2 wt % measured by 27Al MAS NMR. The present invention further relates to a process for producing olefins from alcohols in presence of said catalyst composition. 117.-. (canceled)19. The process for the preparation of a catalyst composition according to further characterized in that said organic acidic medium or an organic medium of step ii.){'sub': 2', '3', '4, 'comprises one or more —COH, —SOH or —SOH groups or salts thereof; or'}is chosen among citric acid, formic acid, oxalic acid, tartaric acid, malonic acid, succinic acid, glutaric acid, adipic acid, maleic acid, phthalic acid, isophthalic acid, fumaric acid, nitrilotriacetic acid, hydroxyethylenediaminetriacetic acid, ethylene di amine tetracetic acid i.e. EDTA, or their corresponding salts being sodium salts or any mixture of thereof.20. The process for the preparation of a catalyst composition according to further characterized in that a calcination is performed before step ii.) said calcination being performed at a temperature lower than 600° C. and with a temperature increase of less than 10° C./min claim 18 , preferably less than 1° C./min for a period of at least 30 min and under a gas flow containing at most 1000 ppm volume of water measured at the inlet of the calcination reactor.21. The process for the preparation of a catalyst composition according to wherein said modified crystalline aluminosilicate of the Framework Type FER has Si/Al framework molar ratio ranging from 25 to 50.22. The process for the preparation of a catalyst ...

METHOD FOR DEHYDRATING ALCOHOLS INTO OLEFINS COMPRISING THE RECYCLING OF ALCOHOLS

This invention relates to a method for dehydration of alcohols into olefins comprising an improved step for recovery of unreacted alcohol. 1. Method for isomerizing dehydration of a feedstock comprising 40 to 100% by weight of primary alcohol substituted in position 2 by an alkyl group comprising at least the following steps:a) Pressurization of said feedstock, followed by the mixing of a fraction of said feedstock, compressed, with the alcohol-rich organic effluent obtained from step h) and with a fraction of the aqueous effluent obtained from step f), and then preheating of said mixture, in such a way as to produce a partially vaporized feedstock, with the residual compressed feedstock fraction being sent to step h);b) Vaporization and final superheating of said partially vaporized feedstock at a temperature of between 250 and 375° C. in such a way as to produce a vaporized feedstock;c) Dehydration of said vaporized feedstock in at least one dehydration reactor that operates in the gas phase at a weighted mean temperature of between 250 and 375° C., at a pressure of between 0.2 MPa and 1 MPa, and at a PPH of between 1 and 18 h−1, in the presence of a catalyst that comprises a zeolite that has at least one series of channels whose opening is defined by a ring with 8 oxygen atoms (8 MR), with said catalyst being coked in advance in-situ or ex-situ, in such a way as to produce a dehydration effluent;d) Cooling of said dehydration effluent obtained from step c) to a temperature of between 30 and 50° C., in such a way as to produce a cooled effluent;e) Separation by decanting of said cooled effluent into an aqueous phase and an organic phase;f) Separation by distilling of said aqueous phase obtained from step e) in such a way as to produce a light hydrocarbon effluent comprising at least 50% by weight of hydrocarbons comprising at most 4 carbon atoms and an aqueous effluent, with a fraction of said aqueous effluent being purged, and the other part being recycled to ...

Process for Preparing Olefins by Dehydrating Alcohols with Less Side Effects Comprising Addition of Organic Acids

The present invention is a process for dehydrating an alcohol to prepare corresponding olefin(s), comprising: 113.-. (canceled)15. The process according to wherein the dehydration unit comprises at least one metallic internal wall.16. The process according to wherein the feed (A)-providing step comprises adding one or more compound(s) chosen among organic acid to the feed (A) or directly in the dehydration unit or contained in a stream recovered from step (c) and recycled back to step (a).17. The process according to claim 14 , wherein the organic acid is at least one compound selected from the group consisting of carboxylic acids claim 14 , in particular carboxylic acids having a carbon chain of 1 to 10 carbon atoms.18. The process according to claim 14 , wherein:the recovery step (c) comprises recovering the one or more unconverted alcohols, the process further comprising, subsequent to recovery step (c), a step of:(d) recycling the unconverted alcohol to the feed (A)-providing step (a), in the dehydration unit.19. The process according to claim 14 , wherein the recovering step (c) comprises recovering the one or more olefin and the one or more unconverted alcohols claim 14 , as well as each compound contained in the effluent (B) claim 14 , by means of fractionating.20. The process according to claim 14 , wherein the one or more alcohols provided in step (a) are bio-alcohol(s) issued from edible or non-edible biomass.21. The process according to claim 14 , wherein the one or more alcohols provided in step (a) are obtained via syn-gas route or synthesized via partial oxidation of paraffin.22. The process according to claim 14 , wherein the one or more alcohols provided in step (a) are produced via hydrogenation of corresponding aldehydes claim 14 , ketones or acids issued from the edible or non-edible biomass.23. The process according to claim 14 , where the one or more olefins recovered in step c) are used for production of polymers and elastomers.24. The process ...

Catalyst composition comprising modified crystalline aluminosilicate for dehydration of alcohols

Process for preparing a catalyst composition containing a modified crystalline aluminosilicate and a binder, wherein the catalyst composition comprises from 5 to 95% by weight of crystalline aluminosilicate as based on the total weight of the catalyst composition, the process being remarkable in that it comprises a step of steaming said crystalline aluminosilicate: at a temperature ranging from 100° C. to 380° C.; under a gas phase atmosphere containing from 5 wt % to 100 wt % of steam; at a pressure ranging from 2 to 200 bars; at a partial pressure of H 2 O ranging from 2 to 200 bars; and said steaming being performed during at least 30 min and up to 144 h; and in that the process also comprises a step of shaping, or of extruding, the crystalline aluminosilicate with a binder, wherein the binder is selected to comprise at least 85 wt % of silica as based on the total weight of the binder, and less than 1000 ppm by weight as based on the total weight of the binder of aluminium, gallium, boron, iron and/or chromium.

CATALYST COMPRISING AN ACTIVE NICKEL PHASE DISTRIBUTED IN A SHELL

Catalyst comprising a nickel-based active phase and an alumina support, characterized in that: 1. A catalyst comprising a nickel-based active phase and an alumina support , said catalyst comprising between 1% and 50% by weight of elemental nickel relative to the total weight of the catalyst , said catalyst being characterized in that:the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst;the nickel density ratio between the crust and the core is strictly greater than 3;said crust comprises more than 25% by weight of nickel element relative to the total weight of nickel contained in the catalyst,the size of the nickel particles in the catalyst, measured in oxide form, is between 7 and 25 nm.2. The catalyst as claimed in claim 1 , wherein the nickel density ratio between the crust and the core is greater than or equal to 3.5.3. The catalyst as claimed in claim 1 , wherein said crust comprises more than 40% by weight of nickel element relative to the total weight of nickel contained in the catalyst.4. The catalyst as claimed in claim 1 , wherein the transition interval between the core and the crust of the catalyst is between 0.05% and 3% of the diameter of the catalyst.5. The catalyst as claimed in claim 1 , characterized in that the size of the nickel particles in the catalyst is between 8 and 23 nm.6. The catalyst as claimed in claim 1 , wherein the sulfur content of the alumina support is between 0.001% and 2% by weight relative to the total weight of the alumina support claim 1 , and the sodium content of said alumina support is between 0.001% and 2% by weight relative to the total weight of said alumina gel.7. The catalyst as claimed in claim 1 , characterized in that the thickness of said crust is between 2.5% and 12% of the diameter of the catalyst.8. The catalyst as claimed in claim 1 , characterized in that the nickel ...

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND N-PROPANOL

The present invention relates to a process for the production of a mixture of ethylene and propylene from a mixture containing ethanol and n-propanol and having a water content comprised between 30 and 75% by weight with respect to the total weight of the mixture. 2. Process according to claim 1 , in which the mixture contains between 1 and 75% by weight of ethanol and between 99 and 25% by weight of n-propanol with respect to the total weight of ethanol and n-propanol.3. Process according to claim 1 , in which the aluminas (A) and (B) are gamma aluminas.4. Process according to claim 1 , in which the alumina (A) has a mean mesopore diameter comprised between 6 and 12 nm and preferably comprised between 7 and 11 nm.5. Process according to claim 1 , in which the alumina (B) has a BET specific surface area measured according to the standard ASTM D 3663-03 comprised between 150 and 180 m/g.6. Process according to claim 1 , in which the alumina (B) has a mean mesopore diameter comprised between 15 and 20 nm.7. Process according to claim 1 , in which before stage a) the mixture is brought into contact with an aromatic cut comprising a mixture of aromatic compounds having 7 to 10 carbon atoms claim 1 , in a separation unit comprising a liquid-liquid extraction column claim 1 , so as to separate from said extraction column an aqueous fraction and an organic fraction containing the aromatic cut claim 1 , ethanol claim 1 , n-propanol and said organic fraction is sent into a distillation column configured in order to provide an effluent containing the aromatic cut and a mixture containing ethanol and n-propanol and said mixture is sent into the dehydration unit.8. Process according to claim 7 , in which the aromatic cut is a mixture of 1 claim 7 ,3 claim 7 ,5-trimethylbenzene and 1 claim 7 ,2 claim 7 ,4-trimethylbenzene.9. Process according to claim 7 , in which the mixture containing ethanol claim 7 , n-propanol and water is brought into contact with the aromatic cut is ...

METHOD FOR THE SELECTIVE HYDROGENATION OF A PYROLYSIS GASOLINE FEEDSTOCK WITH A THREE-PHASE REACTOR

This invention has as its object a method for selective hydrogenation of a feedstock comprising a pyrolysis gasoline carried out in a three-phase reactor. 1. Method for selective hydrogenation of a liquid feedstock comprising a pyrolysis gasoline in the presence of a gaseous phase comprising hydrogen , characterized in that the operation is performed in a three-phase reactor in the presence of a selective hydrogenation catalyst that is dispersed in the liquid phase , with said method being performed at a molar ratio of (hydrogen)/(polyunsaturated compounds to be hydrogenated) of between 0.5 and 10 , at a temperature of between 0° C. and 200° C. , at an hourly volumetric flow rate (V.V.H.)—that is defined as the ratio of the volumetric flow rate of the feedstock at 15° C. to the total volume of the reaction zone—of between 0.5 hand 100 h , and at a pressure of between 1 MPa and 6.5 MPa.2. Method according to claim 1 , in which the selective hydrogenation catalyst is between 1 and 1 claim 1 ,000 μm in size.3. Method according to claim 1 , in which the surface liquid velocity slv of the liquid phase is between 1 mm/s and 10 m/s.4. Method according to claim 1 , in which the concentration of catalyst in the three-phase reactor in relation to the feedstock is between 5% and 40% by weight.5. Method according to claim 1 , which is carried out at a molar ratio of (hydrogen)/(polyunsaturated compounds to be hydrogenated) of between 1 and 2 claim 1 , at a temperature of between 80° C. and 180° C. claim 1 , at an hourly volumetric flow rate (V.V.H.) of between 1 hand 6 h claim 1 , and at a pressure of between 2 MPa and 6 MPa.6. Method according to claim 1 , in which the selective hydrogenation catalyst comprises a metal from group VIII on a porous substrate formed by at least one oxide.7. Method according to claim 1 , comprising the following steps:a) said liquid feedstock and a gaseous phase comprising hydrogen are continuously introduced into a three-phase reactor containing ...

PROCESS FOR THE PRODUCTION OF MIDDLE DISTILLATES FROM A FEEDSTOCK COMPRISING BUTANOL AND PENTANOL

The invention relates to a process for the production of middle-distillate hydrocarbon-containing bases from a feedstock comprising butanol and pentanol, with said process comprising at least: 1. Process for the production of middle-distillate hydrocarbon-containing bases from a feedstock comprising butanol and pentanol , with said process comprising at least:a) A stage for isomerizing dehydration of said feedstock in the presence of an amorphous or zeolitic acid catalyst in at least one reactor, operating at an absolute pressure at the reactor inlet of between 0.5 and 2 MPa and at a temperature at the reactor inlet of between 350 and 450° C. in such a way as to produce an effluent that is for the most part olefinic,b) A stage for separation of the water that is present in said effluent that is for the most part olefinic operating at a pressure of between 0.5 and 1.2 MPa and at a temperature of between 35 and 60° C. in such a way as to obtain at least one organic liquid effluent,c) A stage for purification of the organic liquid effluent coming from stage b) in such a way as to produce a purified organic effluent,{'sup': '−1', 'd) A first stage for selective oligomerization of isobutenes and isopentenes of a feedstock that comprises at least a portion of the purified organic effluent coming from stage c), in the presence of an amorphous catalyst in at least one reactor that operates at an absolute pressure of between 0.5 and 10 MPa, at a temperature at the reactor inlet of between 40 and 95° C., and at an hourly volumetric flow rate of between 0.1 and 10 h, in such a way as to produce a first oligomerization effluent, comprising at least 20% by weight of olefins having a number of carbon atoms that is greater than or equal to 6, with the percentage by weight being expressed relative to the total mass of olefins contained in said effluent,'}{'sup': '−1', 'e) A second stage for oligomerization of said first oligomerization effluent, of the entire effluent coming from ...

Process for pretreatment of vegetable oils by heterogeneous catalysis of the esterification of fatty acids

The invention relates to a continuous process for pretreatment of an oil feedstock comprising at most 20% by weight of free fatty acids by esterification of free fatty acids in which a vertical liquid/liquid contactor containing an esterification catalyst in solid form is supplied in counter-current by an alcohol feedstock comprising at least 20% by weight of an alcohol and said oil feedstock, with said contactor being operated at a temperature of between 25 and 120° C., with said contactor performing the contact in liquid-liquid counter-current between a heavy phase and a light phase, with said heavy phase being able to be either an oil-rich phase or an alcohol-rich phase.

METHOD FOR SIMULTANEOUSLY ELIMINATING ISOBUTANAL AND ETHANOL FROM OLEFINIC FEEDSTOCKS BY ADSORPTION ON A POROUS REFRACTORY OXIDE-BASED MATERIAL

This invention pertains to a method for purifying an olefinic feedstock that comprises olefins with 4 carbon atoms and impurities including isobutanal, ethanol, and acetone, where said method comprises a pretreatment that comprises a step for eliminating acetone and optionally a step for eliminating the water that is present in said olefinic feedstock, and a step for simultaneously eliminating isobutanal and ethanol by running the feedstock obtained from the pretreatment over at least one fixed bed having at least one adsorbent that comprises at least one porous refractory oxide-based material, optionally impregnated with one or more alkaline or alkaline-earth cations; where said step for simultaneously eliminating isobutanal and ethanol operates at a temperature of between 0 and 200° C., at a pressure of 0.1 to 10 MPa, and with an hourly volumetric flow rate (VVH) of the feedstock on the fixed bed of between 0.1 and 10 h. 1. Method for purifying an olefinic feedstock that comprises olefins with 4 carbon atoms and impurities including isobutanal , ethanol , and acetone , wherein said method comprises:a) A pretreatment step that comprises at least one acetone elimination step; andb) A step for simultaneously eliminating isobutanal and ethanol by running the pretreated feedstock obtained from Step a) over at least one fixed bed with at least one adsorbent that comprises at least one porous refractory oxide-based material,{'sup': '−1', 'wherein said Step b) operates at a temperature of between 0 and 200° C., at a pressure of 0.1 to 10 MPa, and with an hourly volumetric flow rate (VVH) of the pretreated feedstock obtained from Step a) over the fixed bed of between 0.1 and 10 h.'}2. Method in accordance with claim 1 , wherein said olefinic feedstock is produced from the dehydration of isobutanol or a mixture of butanol isomers that comprises isobutanol.3. Method in accordance with claim 1 , wherein the pretreatment step also comprises a phase for eliminating the water ...

Catalyst Composition Comprising Modified Crystalline Aluminosilicate for Dehydration

Process for preparing a catalyst composition containing a modified crystalline aluminosilicate and a binder, wherein the catalyst composition comprises from 5 to 95% by weight of crystalline aluminosilicate as based on the total weight of the catalyst composition, the process being remarkable in that it comprises a step of steaming said crystalline aluminosilicate: 115.-. (canceled)17. The process for preparing a catalyst composition according to claim 16 , characterized in that:the binder contains at least 90 wt % of silica as based on the total weight of the binder, and/orthe binder comprises less than 500 ppm by weight as based on the total weight of the binder of aluminium, gallium, boron, iron and/or chromium.18. The process for preparing a catalyst composition according to claim 16 , characterized in that the process further comprises the following steps:not performing any leaching treatment either before step b) or after step c) in order to maintain constant the concentration of aluminium in the modified crystalline aluminosilicate;{'sub': '4', 'Performing an optional step of washing or ion exchange with an alkali metal or NHsalts after step c) or before step b);'}Performing an optional calcination step of the product obtained after step c) or before step b);Performing an optional step of recovering said modified crystalline aluminosilicate after step c).19. The process for preparing a catalyst composition according to claim 16 , characterized in that said crystalline aluminosilicate is a 10 membered ring zeolite of the Framework Type FER claim 16 , MWW claim 16 , EUO claim 16 , MFS claim 16 , ZSM-48 claim 16 , MTT claim 16 , MFI claim 16 , MEL claim 16 , TON or SZR and is chosen among ferrierite claim 16 , FU-9 claim 16 , ISI-6 claim 16 , NU-23 claim 16 , Sr-D claim 16 , ZSM-35 claim 16 , ZSM-57 or SUZ-4 or any mixture thereof.20. The process for preparing a catalyst composition according to claim 16 , characterized in that the step of shaping claim 16 , or ...

PROCESS FOR DEHYDRATION AND ISOMERIZATION OF ALCOHOLS USING A CATALYST BASED ON A MESOSTRUCTURED MATERIAL COMPRISING SILICON

This invention has as its object a process for simultaneous dehydration and skeletal isomerization of a feedstock that comprises at least one Cmonoalcohol and that contains between 0.5 and 50% water, for the purpose of producing Calkenes, with said process operating at a temperature of between 250 and 550° C., under a pressure of between 0.1 and 1 MPa, with an hourly volumetric flow rate of between 0.1 and 10 h-1, characterized in that it uses a catalyst that comprises at least one mesostructured material that comprises silicon and at least one element X that is selected from among aluminum, boron, gallium, indium, and germanium. 1. Process for simultaneous dehydration and skeletal isomerization of a feedstock that comprises at least one Cmonoalcohol and that contains between 0.5 and 50% water , for the purpose of producing Calkenes , with said process being performed at a temperature of between 250 and 500° C. , under a pressure of between 0.1 and 1 MPa , with an hourly volumetric flow rate of between 0.1 and 10 h-1 , characterized in that it uses a catalyst that comprises at least one mesostructured material that comprises silicon and at least one element X that is selected from among aluminum , boron , gallium , indium and germanium.2. Process according to claim 1 , such that said mesostructured material has an Si/X molar ratio of between 0.05 and 1 claim 1 ,000.3. Process according to claim 1 , such that the Si/X molar ratio is between 0.05 and 6.4. Process according to claim 1 , such that the Si/X molar ratio is between 0.05 and 3.5. Process according to claim 1 , such that the Si/X molar ratio is between 15 and 1 claim 1 ,000.6. Process according to claim 1 , such that the Si/X molar ratio is between 15 and 100.7. Process according to claim 1 , such that said feedstock for the most part comprises isobutanol.8. Process according to claim 1 , such that said mesostructured material has a mesostructure that is hexagonal 2D claim 1 , vermicular or cubic 3D.9. ...

Process for recovering alcohols in a fermenter

The present invention concerns a process for recovering fermentation products present in a fermentation mash produced in a bioreactor (9), comprising a step a) in which a gas stream (15) is sent into the fermentation mash under pressure in order to entrain at least a portion of the products and produce a gas stream (16) which is enriched in fermentation products. The process comprises a step h) for storage of the fermentation gases and the gas stream which is sent to the step a) is constituted by the stored fermentation gases.

PROCESS FOR THE STEAM CRACKING OF ETHANE

The invention relates to a process for the steam cracking of a feedstock composed of at least 80% by weight, in particular of at least 90% by weight, of ethane, the process comprising a steam cracking of the feedstock in a furnace (), then a quenching of the pyrolysis products, then a compression operation, then a series of successive operations on the products resulting from the quenching, the said series of operations comprising a washing operation, followed by a drying operation and at least one compression operation, and finally a fractionation by cryogenic distillation. A selective hydrogenation operation, followed by a catalytic conversion operation, will be inserted into the said process, after the drying operation and before the fractionation, in order to partially convert the ethylene predominantly into propylene. 12. Process for the steam cracking of a feedstock composed of at least 80% by weight , in particular of at least 90% by weight , of ethane , the process comprising a steam cracking of the feedstock in a furnace () , then a quenching of the pyrolysis products , then a compression operation , then a series of successive operations on the products resulting from the quenching , the said series of operations comprising a washing operation , followed by a drying operation and at least one compression operation , and finally a fractionation by cryogenic distillation , characterized in that a selective hydrogenation operation , followed by a catalytic conversion operation , is inserted into the said process , after the drying operation and before the fractionation , on the products obtained after drying , in order to partially convert the ethylene predominantly into propylene.2. Process according to claim 1 , characterized in that the ethylene is partially converted into propylene and into other components comprising butene and aromatics.3. Process according to claim 1 , characterized in that the catalytic conversion operation is followed by at least one ...

PROCESS FOR THE PRODUCTION OF KEROSENE FROM BUTANOLS

The invention relates to a process for the production of middle-distillate hydrocarbon-containing bases from a butanol feedstock, with said process comprising at least the following stages: 1. Process for the production of middle-distillate hydrocarbon-containing bases from a butanol feedstock , with said process comprising at least:a) A stage for isomerizing dehydration of said butanol feedstock in the presence of an amorphous or zeolitic acid catalyst in at least one reactor, operating at an absolute pressure at the reactor inlet of between 0.5 and 1.2 MPa and at a temperature at the reactor inlet of between 350 and 450° C. in such a way as to produce an effluent that is for the most part butylene,b) A stage for separation of the water that is present in said butylenic effluent that operates at a pressure of between 0.5 and 1.2 MPa and at a temperature of between 35 and 60° C.,c) A stage for purification of the organic liquid effluent that comes from stage b) in such a way as to produce a purified organic effluent,{'sup': '−1', 'd) A first stage for oligomerization of a feedstock that comprises at least a portion of the purified organic effluent that comes from stage c), the entire effluent that comes from stage g), and at least a portion of the light product that comes from stage 0 in the presence of an amorphous catalyst in at least one reactor that operates at an absolute pressure of between 0.5 and 10 MPa, at a temperature of between 40 and 110° C., and at an hourly volumetric flow rate of between 0.1 and 10 h, in such a way as to produce a first oligomerization effluent, comprising at least 50% by weight of olefins having a number of carbon atoms that is greater than or equal to 8, with the percentage by weight being expressed relative to the total mass of olefins contained in said effluent,'}{'sup': '−1', 'e) A second stage for oligomerization of said first oligomerization effluent, in the presence of an amorphous catalyst in at least one reactor that ...

Process for Dehydration of Mono-Alcohol(s) Using a Modified Crystalline Aluminosilicate

The invention relates to a process for dehydration of a mono-alcohol, or of a mixture of at least two mono-alcohols, having at least 2 carbon atoms and at most 7 carbon atoms into olefins having the same number of carbons, wherein the process uses a catalyst composition that comprises a modified crystalline aluminosilicate has an acidity between 350 and 500 μmol/g that comprises, and further wherein the catalyst composition is obtained by a process comprising the steps of providing a crystalline aluminosilicate having a Si/Al framework molar ratio greater than 10; and steaming said crystalline aluminosilicate, or said shaped and/or calcined crystalline aluminosilicate at a temperature ranging from 100° C. to 380° C.; and under a gas phase atmosphere, without liquid, containing from 5 wt % to 100 wt % of steam; at a pressure ranging from 2 to 200 bars; at a partial pressure of H 2 O from 2 bars to 200 bars; and said steaming being performed during at least 30 min and up to 144 h.

Integrated method for producing butadiene from butanol

The invention relates to a thermally-integrated method for producing butadiene from butanol that comprises at least the following steps: a) Dehydration of butanol, fed by a dehydration feed that is formed from at least said n-butanol feedstock that is diluted with at least a portion of the purified water effluent that is obtained from step c), leading to a butene effluent in at least one reactor, in the presence of a catalyst that comprises an alumina, b) Oxidizing dehydrogenation of said butene effluent, diluted with at least a portion of the purified water effluent that is obtained from step c), into butadiene, with said butene effluent not having undergone any treatment following the dehydration step a), c) Separation of the effluent that is obtained from step b) into at least one butadiene effluent and one purified water effluent.

PROCESS FOR DEHYDRATION OF ETHANOL INTO ETHYLENE USING PRETREATMENT OF THE FEEDSTOCK

The invention relates to a process for dehydration of an ethanol feedstock into ethylene comprising at least the stages: 1. Process for dehydration of an ethanol feedstock into ethylene comprising at least the stages:a) A stage for pretreatment of the ethanol feedstock on an acidic solid operating at a temperature of between 100 and 130° C. in such a way as to produce a pretreated ethanol feedstock,b) A stage for evaporation of an evaporation feedstock comprising said ethanol feedstock that is pretreated in a heat exchanger, with said evaporation feedstock being introduced into said evaporation stage at a pressure of between 0.1 and 2.5 MPa in such a way as to produce an evaporated feedstock,c) A stage for superheating said evaporated feedstock in such a way as to bring it to an inlet temperature that is compatible with the temperature of the dehydration reaction, i.e., to a temperature of between 350 and 550° C.,d) A stage for dehydration of said feedstock that is obtained from stage c) in at least one adiabatic reactor that contains at least one dehydration catalyst and in which the dehydration reaction takes place, operating at an inlet temperature of between 350 and 550° C. and at an inlet pressure of between 0.3 and 1.8 MPa.2. Process according to claim 1 , in which said ethanol feedstock is an ethanol feedstock that is produced from a renewable source that is obtained from biomass.3. Process according to claim 1 , in which said evaporation feedstock is introduced into said evaporation stage b) at a pressure of between 0.1 and 1.4 MPa and comprising a compression stage of said feedstock that is evaporated prior to said super-heating stage c).4. Process according to claim 3 , in which the pressure of the compressed feedstock is between 0.3 and 1.8 MPa.5. Process according to claim 1 , in which said evaporated feedstock claim 1 , optionally compressed claim 1 , is heated in an exchanger of the gas single-phase type claim 1 , using a heat exchange with the ...

METHOD FOR THE ISOMERIZING DEHYDRATION OF A NON-LINEAR PRIMARY ALCOHOL FEEDSTOCK IN THE PRESENCE OF WATER INJECTION AND A CATALYST COMPRISING A FER OR MFS ZEOLITE

A process for the isomerizing dehydration of a feedstock including a primary monoalcohol, alone or as a mixture, of formula R—CH—OH, wherein R is a nonlinear alkyl radical of general formula CHwhere n is an integer between 3 and 20, the process taking place 1. A process for the isomerizing dehydration of a feedstock comprising a primary monoalcohol , alone or as a mixture , of formula R—CH—OH , wherein R is a nonlinear alkyl radical of general formula CHwhere n is an integer between 3 and 20 , said process taking place{'sup': '−1', 'in the gas phase at a weighted average temperature between 275° C. and 400° C., at a pressure between 0.3 MPa and 1 MPa and at a WWH (weight per weight per hour) between 5 and 10 h,'}in the presence of a catalyst comprising at least one silicic binder and at least one zeolite having at least one series of channels, the opening of which is defined by a ring of 8 oxygen atoms (8MR),process wherein vaporized feedstock entering the reactor has a weight content of water of from 4% to 35%.2. The process as claimed in claim 1 , wherein the zeolite is selected from the group formed by FER-type zeolites claim 1 , which are ferrierite claim 1 , FU-9 claim 1 , ISI-6 claim 1 , NU-23 claim 1 , ZSM-35 and the MFS-type zeolite which is ZSM-57 claim 1 , taken alone or as a mixture.3. The process as claimed in claim 1 , wherein said zeolite is ferrierite.4. The process as claimed in claim 1 , wherein the ferrierite has an Si/Al molar ratio of 8 to 70 claim 1 , preferably selected between 10 and 50.5. The process as claimed in claim 1 , wherein the content of zeolite in the catalyst is between 50% and 90% by weight claim 1 , preferably between 60% and 80% by weight.6. The process as claimed in claim 1 , wherein the catalyst contains claim 1 , and preferably consists of claim 1 , a ferrierite and a silicic binder.7. The process as claimed in claim 1 , wherein the catalyst the binder consists of amorphous silica.8. The process as claimed in claim 1 , ...

PROCESS FOR DEHYDRATION OF ETHANOL TO ETHYLENE AT LOW ENERGY CONSUMPTION

A process for dehydration of an ethanol feedstock to ethylene by: 1. Process for dehydration of an ethanol feedstock to ethylene comprising:a) a step of preheating said ethanol feedstock to a temperature comprised between 100 and 130° C. by heat exchange with the effluent from step e),b) a step of pretreating the ethanol feedstock on an acidic solid operating at a temperature comprised between 100 and 130° C. so as to produce a pretreated ethanol feedstock,c) a step of vaporizing a vaporization feedstock comprising said pretreated ethanol feedstock and at least a portion of the flow of treated water recycled according to step h) in an exchanger by means of heat exchange with the effluent from the last reactor of step e), said vaporization feedstock being introduced into said vaporization step at a pressure comprised between 0.1 and 1.4 MPa so as to produce a vaporized feedstock,d) a step of compressing said vaporized feedstock in a compressor so as to produce a compressed feedstock,e) a step of dehydrating said compressed feedstock in at least one adiabatic reactor containing at least one dehydration catalyst and in which the dehydration reaction takes place, operating at an inlet temperature comprised between 350 and 550° C. and at an inlet pressure comprised between 0.3 and 1.8 MPa,f) a step of separating the effluent from the last adiabatic reactor of step e) into an effluent comprising ethylene at a pressure below 1.6 MPa and an effluent comprising water,g) a step of purifying at least a portion of the effluent comprising water from step f) and separating at least one flow of treated water and at least one flow of unconverted ethanol,h) a step of recycling at least a portion of the flow of treated water from step g) upstream of step c).2. Process according to claim 1 , wherein said ethanol feedstock is an ethanol feedstock produced starting from a renewable source obtained from biomass.3. Process according to claim 1 , wherein the vaporization feedstock also ...

Modified Crystalline Aluminosilicate for Dehydration of Alcohols

The present invention relates to a catalyst composition comprising a modified crystalline aluminosilicate of the Framework Type FER having Si/Al framework molar ratio greater than 20 characterized in that in said modified crystalline aluminosilicate the ratio between the strong acid sites and the weak acid sites, S/W, is lower than 1.0 and having the extra framework aluminum (EFAL) content lowered to less than 10 wt % preferably 5 wt % even more preferably less than 2 wt % measured by 27Al MAS NMR. The present invention further relates to a process for producing olefins from alcohols in presence of said catalyst composition. 117.-. (canceled)18. A catalyst composition , for the dehydration of alcohols in olefins having the same number of carbons , comprising a modified crystalline aluminosilicate whereinsaid modified crystalline aluminosilicate is of the Framework Type FER having Si/Al framework molar ratio greater than 20;{'sup': '27', 'in said modified crystalline aluminosilicate the extra framework aluminum, EFAL, content is lower than 15 wt % preferably 10 wt % even more preferably less than 7 wt % measured by Al MAS NMR;'}in said modified crystalline aluminosilicate the ratio between the strong acid sites and the weak acid sites, S/W, is lower than 1.0; the ratio S/W being measured by temperature-programmed desorption of ammonia and being determined by the ratio of the peak area of ammonia desorbed above 340° C. to that desorbed below 340° C.; said crystalline aluminosilicate is not steamed; and', 'said crystalline aluminosilicate is treated with an organic acidic medium and/or an organic medium; and/or', 'strong acid sites of said crystalline aluminosilicate are selectively poisoned with alkali salts or alkaline earth salts or silver so that preferably the weight percent of alkali or alkaline earth or silver on the catalyst composition is of at least 0.5% weight, more preferably at least 1% weight, most preferably at least 5% weight measured by chemical ...

NOVEL DEVICE FOR DISTRIBUTING GAS AND LIQUID IN CATALYTIC DISTILLATION COLUMNS

The present invention describes a device for supplying the catalytic zone of a reactive distillation column using a liquid stream as the reaction stream, the flow of liquid in the reactive zone being of the upflow type and gas not encountering the liquid in the reactive zone. 188345861079123113. A reactive distillation column constituted by alternating catalytic zones () and distillation zones (B) in which , at each of the catalytic zones () , the liquid is introduced upstream of said zone via a central liquid collector comprising a first cylindrical or parallelepipedal portion () followed by a second tubular portion () which brings the liquid into a liquid distribution zone () located below the catalytic zone () and having the same section as said catalytic zone , the liquid then passing through the catalytic zone in upflow mode and being evacuated from said catalytic zone via a peripheral zone () abutting the wall of the column or via a system of vents () passing through the catalytic zone , the gas bypassing the catalytic zone (C) via a dedicated peripheral zone () or via an array of vertical vents () which discharge above the upper level of liquid weirs () , the central collector () being provided with an overflow device the height H of which , precisely defined as the maximum height of liquid between the level of weir of the liquid layer () and the top of the overflow device of the central collector () , has a value in the range 0.2 m to 2 m , preferably in the range 0.3 m to 1 m.269. The reactive distillation column as claimed in claim 1 , in which the liquid is evacuated via a dedicated peripheral zone () claim 1 , and the catalytic zone is bypassed by the gas by means of an array of vents ().3109. The reactive distillation column as claimed in claim 1 , in which the liquid is evacuated via an array of vents () claim 1 , and the catalytic zone is bypassed by the gas by means of an array of vents ().49. The reactive distillation column as claimed in claim 1 , ...

PROCESS FOR THE ISOMERIZING DEHYDRATION OF A PRIMARY ALCOHOL FEEDSTOCK SUBSTITUTED IN POSITION 2 BY AN ALKYL GROUP ON A CATALYST COMPRISING AN IRON-TYPE ZEOLITE

Isomerizing dehydration of feedstock containing a primary alcohol substituted in position 2 by an alkyl group in which the feedstock is heated to the reaction temperature by indirect heat exchange then vaporization by mixing with a diluent effluent, the diluted and vaporized feedstock being dehydrated in at least one dehydration reactor operating in gas phase at an inlet temperature comprised between 250 and 375° C., at a pressure comprised between 0.2 MPa and 1 MPa and at a WHSV comprised between 1 and 18 h, in the presence of a catalyst comprising a zeolite having at least one series of channels the opening of which is defined by a ring with 8 oxygen atoms (8MR) and a binder, the catalyst being coked beforehand in-situ or ex-situ, so as to produce a dehydration effluent, the latter being treated and separated into a diluent effluent, an alkenes effluent and a heavy hydrocarbons effluent. 1. Process for the isomerizing dehydration of a feedstock comprising from 40 to 100% by weight of primary alcohol substituted in position 2 by an alkyl group comprising at least the following steps:a) Pressurization of said feedstock then preheating the compressed feedstock by heat exchange with the dehydration effluent originating from step c) in a heat exchanger so as to produce a preheated feedstock;b) Vaporization of said feedstock preheated by mixing with the diluent effluent originating from step f), the ratio of the diluent effluent mass flow rate to the preheated feedstock being comprised between 5/95 and 60/40;{'sup': '−1', 'c) Dehydration of the effluent originating from step b) in at least one dehydration reactor operating in gas phase at a weighted average temperature comprised between 250 and 375° C., at a pressure comprised between 0.2 MPa and 1 MPa and at a WHSV comprised between 1 and 18 h, in the presence of a catalyst comprising a zeolite having at least one series of channels the opening of which is defined by a ring with 8 oxygen atoms (8MR), said catalyst ...

THERMO-MECHANICALLY INTEGRATED PROCESS FOR THE PRODUCTION OF ETHYLENE OXIDE FROM A FLOW OF ETHANOL

Dehydrating an ethanol feed to form ethylene then oxidation of the ethanol to ethylene oxide: vaporization of an ethanol feed and at least a portion of a flow of diluting water comprising recycled ethanol so as to produce a vaporized feed, compression in a compressor driven by a condensing turbine driven by the steam generated by an oxidation step, dehydration of a mixture of compressed vaporized feed, separation of effluent obtained from dehydration into ethylene and water, purification of at least a portion of effluent containing water and separation into at least a flow of treated water and a flow of diluting water containing ethanol, recycling the latter upstream of the vaporization, oxidation of ethylene containing in the effluent into ethylene oxide, in at least one tubular oxidation reactor cooled by vaporization of a quench flow, said vaporized quench flow being used to drive a condensing turbine. 1. A process for the dehydration of an ethanol feed to ethylene then oxidation of the ethylene to ethylene oxide , comprising:a) optionally preheating said ethanol feed to a temperature in the range 70° C. to 130° C. by exchange of heat with the effluent obtained from e);b) optionally pre-treatment of the ethanol feed over an acidic solid operating at a temperature in the range 70° C. to 130° C. in order to produce a pre-treated ethanol feed;c) vaporization of a vaporization feed comprising said pre-treated ethanol feed and at least a portion of the flow of diluting water comprising ethanol recycled to the outlet from g) to an exchanger by means of an exchange of heat with the effluent obtained from the last reactor of e), said vaporization feed being introduced into said vaporization at a pressure in the range 0.1 to 1.4 MPa so as to produce a vaporized feed;d) compressing and superheating said vaporized feed in a compressor so as to produce a feed which is compressed and at the temperature for supplying to dehydration e), said compressor being driven by a ...

Process for Preparing Olefins by Dehydrating Alcohols with Less Side Effects Comprising Addition of Sulfur Containing Compounds

The present invention is a process for dehydrating an alcohol to prepare a corresponding olefin, comprising: (a) providing a composition (A) comprising at least an alcohol having at least 2 carbon atoms, optionally water, optionally an inert component, in a dehydration unit, (b) placing the composition (A) into contact with an acidic catalyst in a reaction zone of said dehydration unit at conditions effective to dehydrate at least a portion of the alcohol to make a corresponding olefin, (c) recovering from said dehydration unit an effluent (B) comprising : at least an olefin, water, undesired by-products including aldehydes and light products, optionally unconverted alcohol(s), optionally the inert component, wherein, said composition (A)-providing step (a) comprises adding an effective amount of one or more sulfur containing compound capable to reduce the undesired by-products by comparison with a non introduction of such sulfur containing compound. The component introduced at step (a) can be chosen from the group consisting of thiols, sulfides, disulfides.

THERMALLY INTEGRATED PROCESS FOR THE PRODUCTION OF ETHYLENE OXIDE FROM A FLOW OF ETHANOL

Process for dehydrating an ethanol feed to ethylene then oxidating the ethanol to ethylene oxide, comprising vaporizing the feed and a flow of diluting water comprising recycled ethanol to produce a vaporized feed, dehydrating a mixture of vaporized feed and a vaporized flow of diluting water comprising ethanol, separating the dehydration effluent into ethylene and water effluents, purifying at least a portion of the water effluent and separating a flow of treated water and a flow of diluting water comprising ethanol, recycling and vaporizing at least a portion of the separated diluting water by partial or complete vaporization in an exchanger using heat exchange with a quench flow obtained from the oxidation, said quench flow, cooled, then recycled to the oxidation reactor(s), and oxidation of the ethylene in the effluent comprising ethylene into ethylene oxide, this oxidation using a tubular oxidation reactor cooled by vaporization of said quench flow. 1. A process for the dehydration of an ethanol feed to ethylene then oxidation of the ethylene to ethylene oxide , comprising:a) an optional step for preheating said ethanol feed to a temperature in the range 70° C. to 130° C. by heat exchange with the effluent obtained from step e);b) an optional step for pre-treatment of the ethanol feed over an acidic solid operating at a temperature in the range 70° C. to 130° C. in order to produce a pre-treated ethanol feed;c) a step for vaporization of a vaporization feed comprising said pre-treated ethanol feed and at least a portion of the flow of diluting water comprising ethanol recycled in accordance with step h) to an exchanger by means of an exchange of heat with the effluent obtained from the last reactor of step e), said vaporization feed being introduced into said vaporization step at a pressure in the range 0.1 to 1.4 MPa so as to produce a vaporized feed;d) a step for compressing and superheating said vaporized feed in a compressor so as to produce a feed which is ...

METHOD FOR SIMULTANEOUSLY ELIMINATING ISOBUTANAL AND A FEEDSTOCKS BY ADSORPTION ON A ZEOLITE MATERIAL

A process for purifying an olefinic feedstock containing olefins with 4 carbon atoms and impurities including isobutanal, ethanol and acetone, the process including a pre-treatment containing at least one step of eliminating the ethanol and the water present in the olefinic feedstock and a step of simultaneously eliminating the isobutanal and the acetone, by passing the feedstock from the pre-treatment over at least one fixed bed of at least one adsorbent containing at least one material with a zeolite framework, the material with a zeolite framework being chosen from zeolites, AIPOs, SAPOs and mixtures thereof; the step of simultaneously eliminating the isobutanal and the acetone being carried out at a temperature of between 0 and 200° C., at a pressure of 0.1 to 10 MPa and with an hourly space velocity of the feedstock over the fixed bed of 0.1 to 10 h. 1. A process for purifying an olefinic feedstock comprising olefins with 4 carbon atoms and impurities including isobutanal , ethanol and acetone , said process comprising:a) a pre-treatment step comprising at least a step of eliminating the ethanol and water;b) a step of simultaneously eliminating the isobutanal and the acetone, by passing the pretreated feedstock from step a) over at least one fixed bed of at least one adsorbent comprising at least one material with a zeolite framework,said material with a zeolite framework being chosen from the group consisting of: zeolites, AlPOs, SAPOs and mixtures thereof;said material with a zeolite framework having at least cages or channels of which at least one opening is defined by a ring comprising at least 10 oxygen atoms (10MR);{'sup': '−1', 'said step b) being carried out at a temperature of between 0 and 200° C., at a pressure of 0.1 to 10 MPa and with an hourly space velocity (HSV) of the pretreated feedstock from step a) over the fixed bed of between 0.1 and 10 h.'}2. The process as claimed in claim 1 , wherein said olefinic feedstock results from the dehydration ...

ALTERNATE PROCESS FOR OLEFIN METATHESIS

Alternated process for olefin metathesis

Process for oligomerizing olefins using a catalyst based on silica-alumina

A process for oligomerizing an olefinic hydrocarbon feed is described which consists of bringing said feed into contact with a catalyst comprising a silica-alumina, the silica content of said catalyst being in the range 5% to 95% by weight, said catalyst being prepared using a process comprising at least: a) mixing at least one alumina compound which is partially soluble in an acid medium with either at least one silica compound which is completely soluble in the reaction mixture or a combination formed by at least one silica compound and at least one alumina compound, said silica and alumina compounds being completely soluble in the reaction mixture, in order to form a solid precursor of said catalyst; b) hydrothermal treatment of the solid derived from step a) by calcining in moist air for a period in the range 4 to 7 hours.

PROCESS FOR THE PREPARATION OF MULTIMETALLIC CATALYSTS FOR USE IN HYDROCARBON PROCESSING REACTIONS

Process for preparing olefins by dehydrating alcohols with less side effects comprising addition of organic acids

The present invention is a process for dehydrating an alcohol to prepare corresponding olefin(s), comprising: (a) providing a feed (A) comprising at least an alcohol having at least 2 carbon atoms, and preferably at most 5 carbon atoms, or a mixture thereof optionally water, optionally an inert component, in a dehydration unit, (b) placing the feed (A) into contact with an acidic catalyst in a reaction zone of said dehydration unit at conditions effective to dehydrate at least a portion of the alcohol to make an olefin or a mixture of olefins having the same number of carbon atoms as the alcohol, (c) recovering from said dehydration unit an effluent (B) comprising : - an olefin or a mixture of olefins, - water, - undesired by-products including aldehydes and lighter products resulting from degradation of said aldehydes under the conditions of step (b), - optionally unconverted alcohol(s) if any, - optionally the inert component, wherein, said feed (A)-providing step (a) comprises adding an effective amount of one or more organic compound capable to reduce the undesired by-products by comparison with a non introduction of such compound, said organic compound being chosen among organic acids.

Simultaneous dehydration and skeletal isomerisation of isobutanol on ti-containing zeolite catalysts

The present invention (in a first embodiment) relates to a process for the simultaneous dehydration and skeletal isomerisation of isobutanol to make substantially corresponding olefins, having the same number of carbons and consisting essentially of a mixture of n-butenes and iso-butene, said process comprising: a) introducing in at least one reactor a feed (A) comprising isobutanol, optionally water, optionally an inert component, b) contacting said feed (A) with a catalyst in said at least one reactor at conditions effective to dehydrate and skeletal isomerise at least a portion of the isobutanol to make a mixture of n-butenes and iso-butene, c) recovering from said at least one reactor an effluent (B) and removing water, the inert component if any and unconverted isobutanol if any to get a mixture of n-butenes and iso-butene , Wherein, the catalyst comprises a Ti-containing zeolite, in which Ti atoms occupy framework positions of the zeolite, said catalyst being capable to make simultaneously the dehydration and skeletal isomerization of butene.

Process for preparing olefins by dehydrating alcohols with less side effects comprising addition of sulfur containing compounds

The present invention is a process for dehydrating an alcohol to prepare a corresponding olefin, comprising: (a) providing a composition (A) comprising at least an alcohol having at least 2 carbon atoms, optionally water, optionally an inert component, in a dehydration unit, (b) placing the composition (A) into contact with an acidic catalyst in a reaction zone of said dehydration unit at conditions effective to dehydrate at least a portion of the alcohol to make a corresponding olefin, (c) recovering from said dehydration unit an effluent (B) comprising: at least an olefin, water, undesired by-products including aldehydes and light products, optionally unconverted alcohol(s), optionally the inert component, wherein, said composition (A)—providing step (a) comprises adding an effective amount of one or more sulfur containing compound capable to reduce the undesired by-products by comparison with a non introduction of such sulfur containing compound. The component introduced at step (a) can be chosen from the group consisting of thiols, sulfides, disulfides.

Process for preparing olefins by dehydrating alcohols with less side effects comprising addition of organic acids

The present invention is a process for dehydrating an alcohol to prepare corresponding olefin(s), comprising: (a) providing a feed (A) comprising at least an alcohol having at least 2 carbon atoms, and preferably at most 5 carbon atoms, or a mixture thereof optionally water, optionally an inert component, in a dehydration unit, (b) placing the feed (A) into contact with an acidic catalyst in a reaction zone of said dehydration unit at conditions effective to dehydrate at least a portion of the alcohol to make an olefin or a mixture of olefins having the same number of carbon atoms as the alcohol, (c) recovering from said dehydration unit an effluent (B) comprising: an olefin or a mixture of olefins, water, undesired by-products including aldehydes and lighter products resulting from degradation of said aldehydes under the conditions of step (b), optionally unconverted alcohol(s) if any, optionally the inert component, wherein, said feed (A)-providing step (a) comprises adding an effective amount of one or more organic compound capable to reduce the undesired by-products by comparison with a non introduction of such compound, said organic compound being chosen among organic acids.

Process for dehydration and isomerization of c4 alcohols using an amorphous solid with suitable porosity

The subject matter of the present invention is a process for producing C4 olefins from a C4 monoalcohol feedstock, in which a reaction for dehydration of the monoalcohol to give at least one olefin, and a reaction for skeletal isomerization of at least one of the olefins produced, are carried out in the same reaction chamber, in the presence of a catalyst based on alumina with suitable porosity.

METHOD FOR CONVERTING CHARGES FROM RENEWABLE SOURCES WITH PRETREATMENT OF LOADS BY HOT DEPHOSPHATION

Process for the conversion of feedstock obtained from renewable sources comprising a pretreatment of said feedstock by hot dephospatation

L'invention concerne un procédé de prétraitement d'une huile végétale ou animale brute consistant en le passage de ladite huile dans un réacteur comprenant au moins un lit fixe d'au moins un adsorbant comprenant un oxyde réfractaire poreux dépourvu de métaux catalytiques, à une température comprise entre 130°C et 320°C, à une pression comprise entre 0,1 et 7 MPa et avec un temps de séjour de ladite huile sur ledit lit fixe compris entre 0,1 et 1 heure. L'invention concerne un procédé de prétraitement d'huile végétale ou animale semi raffinée, intégré en amont d'une étape d'hydrotraitement pour la production de gazole vert. The invention relates to a process for pre-treating a crude vegetable or animal oil consisting in the passage of said oil in a reactor comprising at least one fixed bed of at least one adsorbent comprising a porous refractory oxide free of catalytic metals, at a temperature of temperature between 130 ° C and 320 ° C, at a pressure between 0.1 and 7 MPa and with a residence time of said oil on said fixed bed between 0.1 and 1 hour. The invention relates to a pretreatment process for semi-refined vegetable or animal oil, integrated upstream of a hydrotreatment stage for the production of green gas oil.

Process for producing a tertiary olefin by decomposing a tertiary alkylether, comprising a first step of purification by washing with water

A process for producing a tertiary olefin by decomposing an ether comprises a) decomposing an ether to a product containing an alcohol and a tertiary olefin, b) purifying at least a portion of the product from a) in a water washing extraction zone (L1) to obtain an aqueous fraction (A1) containing the major portion of the alcohol and a fraction (B1) containing the major portion of the tertiary olefin, the fraction (B1) containing the tertiary olefin, water, possibly ether and light compounds and being substantially free of alcohol, and c) in which at least a portion of the fraction (B1) from b) is sent to a separation zone (Co1) from which a liquid aqueous fraction (La1) and a liquid fraction (Lb1) containing the major portion of the tertiary olefin, possibly ether and possibly light compounds, are recovered.

Method for isomerizing dehydration of a primary alcohol substituted in position 2 by an alkyl group on a catalyst comprising an iron zeolite

REACTIONAL ZONE COMPRISING TWO PARALLEL RISERS AND A COMMON SOLID GAS SEPARATION AREA FOR THE PRODUCTION OF PROPYLENE

PROCESS FOR PRODUCING ETHYLENE OXIDE FROM A THERMALLY INTEGRATED ETHANOL FLOW

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène puis d'oxydation de l'éthylène en oxyde d'éthylène comprenant une étape de vaporisation d'une charge comprenant ladite charge éthanol et au moins une partie d'un flux d'eau de dilution comprenant de l'éthanol recyclé de manière à produire une charge vaporisée, une étape de déshydratation d'un mélange comprenant ladite charge vaporisée et un flux vaporisé d'eau de dilution comprenant de l'éthanol, une étape de séparation de l'effluent issu de l'étape de déshydratation en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau, une étape de purification d'au moins une partie de l'effluent comprenant de l'eau et la séparation en au moins un flux d'eau traitée et un flux d'eau de dilution comprenant de l'éthanol, une étape de recyclage et de vaporisation d'au moins une partie du flux d'eau de dilution comprenant de l'éthanol issu de l'étape de séparation par vaporisation partielle ou totale dans un échangeur grâce a un échange de chaleur avec un flux de trempe issu de l'étape d'oxydation, ledit flux de trempe, refroidi, étant ensuite recyclé vers le ou les réacteurs de l'étape d'oxydation, et une étape d'oxydation de l'éthylène compris dans l'effluent comprenant de l'éthylène en oxyde d'éthylène, cette étape d'oxydation comprenant au moins un réacteur tubulaire d'oxydation refroidi par vaporisation dudit flux de trempe. The invention relates to a process for the dehydration of an ethanol feedstock to ethylene and then to the oxidation of ethylene to ethylene oxide comprising a step of vaporizing a feedstock comprising said feedstock ethanol and at least a part of a feedstock. dilution water comprising ethanol recycled to produce a vaporized charge, a step of dehydrating a mixture comprising said vaporized charge and a vaporized ...

METHOD FOR DEHYDRATING ETHYLENE ETHYLENE WITH LOW ENERGY CONSUMPTION

L'invention décrit un procédé de déshydratation d'une charge éthanol en éthylène comprenant la vaporisation de ladite charge éthanol en mélange avec au moins une partie du flux d'eau purifié recyclé selon l'étape f) dans un échangeur grâce à un échange de chaleur avec l'effluent issu du dernier réacteur, ledit mélange étant introduit dans ladite étape de vaporisation à une pression comprise entre 0,1 et 0,4 MPa, la compression du mélange vaporisé dans un compresseur, l'introduction du mélange vaporisée et comprimée, à une température d'entrée comprise entre 350 et 500°C et à une pression d'entrée comprise entre 0,2 et 1,3 MPa, dans au moins un réacteur adiabatique contenant au moins un catalyseur de déshydratation et dans lequel la réaction de déshydratation a lieu, la séparation de l'effluent issu du dernier réacteur adiabatique de l'étape c) en un effluent comprenant de l'éthylène à une pression inférieure à 1 MPa et un effluent comprenant de l'eau, la purification d'au moins une partie de l'effluent comprenant de l'eau issu de l'étape d) et la séparation d'au moins un flux d'eau purifiée et d'au moins un flux d'éthanol non converti, le recyclage d'au moins une partie du flux d'eau purifiée issu de l'étape e) en amont de l'étape a). The invention describes a process for dehydrating an ethylene ethanol feedstock comprising vaporizing said ethanol feedstock in admixture with at least a portion of the stream of purified water recycled according to step f) in an exchanger by means of a feedstock exchange. heat with the effluent from the last reactor, said mixture being introduced into said vaporization step at a pressure of between 0.1 and 0.4 MPa, compressing the vaporized mixture in a compressor, introducing the vaporized and compressed mixture , at an inlet temperature of between 350 and 500 ° C and at an inlet pressure of between 0.2 and 1.3 MPa, in at least one ...

PROCESS FOR THE PREPARATION OF ALCOHOLIC ESTERS AND GLYCERIN FROM TRIGLYCERIDES AND ALCOHOLS USING A HETEROGENEOUS CATALYST IN THE PRESENCE OF CONTROLLED CONTENT WATER

Un procédé de préparation d'une composition d'esters alcooliques d'acides monocarboxyliques linéaires de 6 à 26 atomes de carbone et de glycérine à partir d'une huile végétale ou animale, neutre ou acide, vierge ou recyclée, avec des monoalcools de 1 à 18 atomes, en présence d'un catalyseur aluminate de zinc et en présence d'une teneur contrôlée en eau permettant d'obtenir directement, en une ou plusieurs étapes, un ester utilisable comme carburant ou combustible et une glycérine de pureté améliorée contenant une teneur abaissée en éthers. A process for preparing a composition of alcoholic esters of linear monocarboxylic acids of 6 to 26 carbon atoms and glycerin from a virgin or recycled viral or virgin vegetable or animal oil with monoalcohols of 1 at 18 atoms, in the presence of a zinc aluminate catalyst and in the presence of a controlled water content allowing to obtain directly, in one or more steps, an ester which can be used as fuel or fuel and a glycerin of improved purity containing a lowered content in ethers.

CATALYST INCLUDING AN ACTIVE PHASE OF NICKEL IN THE FORM OF SMALL PARTICLES DISTRIBUTED AS A CRUST

Catalyseur comprenant une phase active à base de nickel et un support d’alumine caractérisé en ce que :- le nickel est réparti à la fois sur une croûte en périphérie du support, et à cœur du support, l'épaisseur de ladite croûte étant comprise entre 2% et 15% du diamètre du catalyseur ;- le ratio de densité en nickel entre la croûte et le cœur est supérieur strictement à 3 ;- ladite croûte comprend entre 40% et 80% en poids en élément nickel par rapport au poids total de nickel contenu dans le catalyseur ;- la taille des particules de nickel dans le catalyseur est inférieure à 7 nm. Catalyst comprising an active phase based on nickel and an alumina support characterized in that: - the nickel is distributed both on a crust at the periphery of the support, and at the heart of the support, the thickness of said crust being included between 2% and 15% of the diameter of the catalyst; - the nickel density ratio between the crust and the core is strictly greater than 3; - said crust comprises between 40% and 80% by weight of nickel element relative to the total weight of nickel contained in the catalyst; - the size of the nickel particles in the catalyst is less than 7 nm.

METHOD FOR CONVERTING CHARGES FROM RENEWABLE SOURCES WITH PRETREATMENT OF CHARGES BY HOT DEPHOSPHATION

L'invention concerne un procédé de prétraitement d'une huile végétale ou animale brute consistant en le passage de ladite huile dans un réacteur comprenant au moins un lit fixe d'au moins un adsorbant comprenant un oxyde réfractaire poreux dépourvu de métaux catalytiques, à une température comprise entre 130°C et 320°C, à une pression comprise entre 0,1 et 7 MPa et avec un temps de séjour de ladite huile sur ledit lit fixe compris entre 0,1 et 1 heure. L'invention concerne un procédé de prétraitement d'huile végétale ou animale semi raffinée, intégré en amont d'une étape d'hydrotraitement pour la production de gazole vert. The invention relates to a process for pre-treating a crude vegetable or animal oil consisting in the passage of said oil in a reactor comprising at least one fixed bed of at least one adsorbent comprising a porous refractory oxide free of catalytic metals, at a temperature of temperature between 130 ° C and 320 ° C, at a pressure between 0.1 and 7 MPa and with a residence time of said oil on said fixed bed between 0.1 and 1 hour. The invention relates to a pretreatment process for semi-refined vegetable or animal oil, integrated upstream of a hydrotreatment stage for the production of green gas oil.

DEVICE FOR PROVIDING A SEPARATE INJECTION AND A HOMOGENEOUS DISTRIBUTION OF TWO FLUIDS

Hydrocarbon catalytic treatment reactor with semi-continuous catalyst replacement

La présente invention concerne un réacteur 1,2 de traitement catalytique d’hydrocarbures, notamment à circulation radiale, comprenant un lit de catalyseur fixe et avec régénération périodique du catalyseur in situ, tel que ledit réacteur est en connexion fluidique, d’une part, en amont, avec un système 31,32 de chargement partiel de catalyseur frais, et, d’autre part, en aval, avec un système 33,34 de déchargement partiel de catalyseur usé, lesdits systèmes venant remplacer une partie seulement du catalyseur usé du réacteur par du catalyseur frais après au moins une, de préférence chaque, régénération in situ du catalyseur. Figure 2 à publier The present invention relates to a reactor 1,2 for the catalytic treatment of hydrocarbons, in particular with radial circulation, comprising a fixed catalyst bed and with periodic regeneration of the catalyst in situ, such that said reactor is in fluid connection, on the one hand, upstream, with a system 31,32 for partial loading of fresh catalyst, and, on the other hand, downstream, with a system 33,34 for partial unloading of spent catalyst, said systems replacing only part of the spent catalyst from the reactor with fresh catalyst after at least one, preferably each, in situ regeneration of the catalyst. Figure 2 to publish

PROCESS FOR THE DEHYDRATION AND ISOMERIZATION OF C4 ALCOHOLS USING AN AMORPHOUS SOLID WITH ADAPTED POROSITY

METHOD FOR ISOMERIZING DEHYDRATION OF NON-LINEAR PRIMARY ALCOHOL ON A CATALYST COMPRISING IRON TYPE ZEOLITHE AND ALUMINUM BINDER

L'invention concerne un procédé de déshydratation isomérisante d'une charge comprenant au moins un monoalcool primaire, seul ou en mélange, de formule R-CH2-OH, dans lequel R est un radical alkyl non linéaire de formule générale CnH2n+1 où n est un entier compris entre 3 et 20, ledit procédé opérant en phase gaz à une température moyenne pondérée comprise entre 200°C et 275°C, à une pression compise entre 0,1 MPa et 1 MPa et à une PPH (poids par poids par heure) comprise entre 1 et 18 h-1, en présence d'un catalyseur comprenant au moins une zéolithe sous forme H ou NH4 présentant au moins une série de canaux dont l'ouverture est définie par un anneau à 8 atomes d'oxygène (8MR), ladite zéolite étant mise en forme avec au moins un liant aluminique, ledit liant est dépourvu d'au moins l'un des éléments choisi indépendamment parmi le Si, Ti, Zr, F, Cl, Br, et I. L'invention concerne également ledit catalyseur et un procédé de préparation. The invention relates to a process for the isomerizing dehydration of a feedstock comprising at least one primary monoalcohol, alone or as a mixture, of formula R-CH 2 -OH, in which R is a non-linear alkyl radical of general formula CnH 2n + 1 where n is an integer between 3 and 20, said method operating in the gas phase at a weighted average temperature of between 200 ° C and 275 ° C, at a pressure of between 0.1 MPa and 1 MPa and a PPH (weight by weight) per hour) of between 1 and 18 h -1, in the presence of a catalyst comprising at least one zeolite in H or NH 4 form having at least one series of channels whose opening is defined by an 8-atom oxygen ring (8MR), said zeolite being shaped with at least one aluminum binder, said binder is devoid of at least one of the elements independently selected from Si, Ti, Zr, F, Cl, Br, and I. L The invention also relates to the catalyst and a method of preparation.

PROCESS FOR PRETREATMENT OF HETEROGENEOUS CATALYSIS VEGETABLE OILS OF ESTERIFICATION OF FATTY ACIDS

L'invention concerne un procédé continu de prétraitement d'une charge huile comprenant au plus 20% poids d'acides gras libres par estérification des acides gras libres dans lequel un contacteur liquide/liquide vertical contenant un catalyseur d'estérification sous forme solide est alimenté à contre-courant par une charge alcool comprenant au moins 20% poids d'un alcool et ladite charge huile, ledit contacteur étant opéré à une température comprise entre 25 et 120°C, ledit contacteur opérant le contact à contre-courant liquide-liquide entre une phase lourde et une phase légère, ladite phase lourde pouvant être soit une phase riche en huile, soit une phase riche en alcool.

PROCESS FOR PRODUCING KEROSENE FROM BUTANOLS

METHOD FOR SELECTIVE HYDROGENATION OF A PYROLYTIC ESSENCE LOAD WITH A THREE-PHASE REACTOR

La présente invention a pour objet un procédé d'hydrogénation sélective d'une charge comportant une essence de pyrolyse effectué dans un réacteur triphasique. The present invention relates to a process for selectively hydrogenating a feedstock comprising a pyrolysis gasoline carried out in a three-phase reactor.

ZINC SUPER-STOICHIOMETRIC ZINC ALUMINATE SPINEL HETEROGENEUS CATALYST AND USE THEREOF IN A PROCESS FOR THE PREPARATION OF ALCOHOL ESTERS FROM TRIGLYCERIDES AND ALCOHOLS

PROCESS FOR THE SELECTIVE HYDROGENATION OF A PYROLYSIS FUEL CHARGE WITH A THREE-PHASE REACTOR

La présente invention a pour objet un procédé d'hydrogénation sélective d'une charge comportant une essence de pyrolyse effectué dans un réacteur triphasique. The present invention relates to a process for the selective hydrogenation of a charge comprising a pyrolysis gasoline carried out in a three-phase reactor.

Production of ether and olefin from an hydrocarbon feed containing a tertiary olefin

The production of ether and olefin from an hydrocarbon feed containing a tertiary olefin is claimed. It consists of several steps: (a) synthesis of the tertiary alkyl ether by contacting a hydrocarbon feed containing a tertiary olefin with an alcohol in a contact zone, in the presence of a catalyst; (b) separation step of the product resulted from step (a) in an organic fraction O1 deficient in tertiary alkyl ether and an organic fraction E1 rich in tertiary alkyl ether; (c) decomposition of the tertiary alkyl ether of the organic fraction E1 of step (b) in a reaction zone R1 in the presence of catalyst into a product P1 containing an alcohol and a tertiary olefin; (d) purification step of the product P1 resulting from step (c) in an extraction zone (L1) by washing with water where A1 containing most of the alcohol and B1 ther tertiary olefin are obtained; (e) recovery of the aqueous liquid fraction La1 from the separation zone (Co1) where B1 is fed and the organic liquid fraction Lb1 containing the tertiary olefin, ether and low and high molecular weight compounds; and (f) feeding of the fraction A1 from step (d) to a fractionating zone (D3) from which G1 fraction containing most of the alcohol and an aqueous fraction (H1) almost alcohol free are recovered. Preferably part of the aqueous fraction La1 and the aqueous fraction (H1) are recycled towards the water extraction zone (L1) of step (d). Part of the fraction G1 is sent to the ether synthesis zone (R100) of step (a). The water extraction zone L1 and L2 contain means of introducing water. Part of the organic fraction Lb1 of step (e) is sent in a fractionating zone D1 from which a fraction E10 containing most of the un-decomposed ether from step (c) and a fraction F1 containing most of the tertiary olefin are recovered. The E10 fraction is recycled in the step (c) zone. Part of the F1 fraction is sent to a fractionating zone D2 from which Lg1 fraction containing most of the low molecular weight compounds and ...

PROCESS FOR PRETREATMENT OF HETEROGENEOUS CATALYSIS VEGETABLE OILS OF ESTERIFICATION OF FATTY ACIDS

METHOD AND METHOD FOR CONVERTING ETHYLENE PRESENT IN THE HEAD EFFLUENT OF AN FCC TO INCREASE PROPYLENE PRODUCTION

La présente invention décrit un procédé de fractionnement de la fraction gazeuse sortant en tête de la colonne de fractionnement d'une unité de craquage catalytique (FCC) utilisant une unité de conversion de l'éthylène en propylène qui permet de valoriser l'éthylène contenu dans le gaz combustible. The present invention describes a process for fractionating the gaseous fraction exiting at the top of the fractionation column of a catalytic cracking unit (FCC) using a unit for converting ethylene to propylene which makes it possible to recover the ethylene contained in the combustible gas.

PROCESS FOR SEPARATING PROPANE AND PROPYLENE USING A DISTILLER COLUMN AND A MEMBRANE SEPARATION UNIT

PROCESS FOR CLEANING A SOLID FERMENTAL REACTOR SUPPORT CONTAINING CONTAMINATED POLYURETHANE FOAM

La présente invention concerne un procédé de nettoyage d'un support solide de réacteur fermentaire pour la production d'alcools par voie fermentaire à partir d'un fluide sucré, le support solide comprenant une mousse de polyuréthane inoculée par une biomasse produite par une souche solvantogène appartenant au genre Clostridium, le procédé comprenant la mise en contact du support solide avec un fluide issu du moût fermentaire enrichi en alcool et/ou acétone et/ou une solution aqueuse à pH basique. The present invention relates to a method for cleaning a solid support for a fermentation reactor for the production of alcohols by fermentation from a sweet fluid, the solid support comprising a polyurethane foam inoculated with a biomass produced by a solvent-producing strain. belonging to the genus Clostridium, the process comprising bringing the solid support into contact with a fluid obtained from the fermentation must enriched in alcohol and / or acetone and / or an aqueous solution at basic pH.

HYDROGENOLYSIS CATALYST OBTAINED FROM MOLTEN SALTS AND AN ORGANIC ADDITIVE

Catalyseur d’hydrogénolyse susceptible d’être obtenu par le procédé comprenant au moins les étapes suivantes :a) on met en contact le support d’alumine avec au moins un additif organique ;b) on met en contact le support d’alumine avec au moins un sel métallique de nickel et au moins un sel métallique de molybdène ;c) on chauffe sous agitation le mélange solide obtenu à l’issue des étapes a) et b) ;d) on sèche le précurseur de catalyseur à l’issue de l’étape c) ;e) on réalise une étape de traitement thermique du précurseur de catalyseur séché obtenu à l’issue de l’étape d).

METHOD FOR DEHYDRATION AND ISOMERIZATION OF ALCOHOLS USING A CATALYST BASED ON MESOSTRUCTURE MATERIAL COMPRISING SILICON

PROCESS FOR THE PRODUCTION OF ALKYL ESTERS FROM VEGETABLE OR ANIMAL OIL AND ALIPHATIC MONOALCOOL WITH HOT PURIFICATION IN FIXED BED.

METHOD AND DEVICE FOR TREATING A CHARGE COMPRISING BUTADIENE

The invention concerns a process and apparatus for treating a feed comprising ethylenic and acetylenic compounds. In the process of the invention, the feed is sent to a distillation step, a C4 cut and a C5+ cut are recovered, a drawn fraction comprising acetylenic compounds is treated in at least one hydrogenation step, and an effluent which is depleted in acetylenic compounds is recycled. The distillation step comprises: an initial step for pre-fractionating the feed, carried out in a pre-fractionation zone included in a distillation column; and at least one complementary fractionation step, carried out in a zone which comprises a portion A, which is distinct from and not adjacent to the portion B of the pre-fractionation zone below the supply, in which the fraction drawn from a point in A is recovered with a C4/C5+ ratio that is higher than that of the feed.

CATALYST INCLUDING AN ACTIVE PHASE OF NICKEL IN THE FORM OF SMALL PARTICLES DISTRIBUTED AS A CRUST

Catalyseur comprenant une phase active à base de nickel et un support d’alumine caractérisé en ce que :- le nickel est réparti à la fois sur une croûte en périphérie du support, et à cœur du support, l'épaisseur de ladite croûte étant comprise entre 2% et 15% du diamètre du catalyseur ;- le ratio de densité en nickel entre la croûte et le cœur est supérieur strictement à 3 ;- ladite croûte comprend entre 40% et 80% en poids en élément nickel par rapport au poids total de nickel contenu dans le catalyseur ;- la taille des particules de nickel dans le catalyseur est inférieure à 7 nm. Catalyst comprising an active phase based on nickel and an alumina support characterized in that: - the nickel is distributed both on a crust at the periphery of the support, and at the heart of the support, the thickness of said crust being included between 2% and 15% of the diameter of the catalyst; - the nickel density ratio between the crust and the core is strictly greater than 3; - said crust comprises between 40% and 80% by weight of nickel element relative to the total weight of nickel contained in the catalyst; - the size of the nickel particles in the catalyst is less than 7 nm.

Performing dehydration and simultaneous skeletal isomerization of isobutanol comprising monohydric alcohol to produce olefinic hydrocarbons, comprises utilizing catalyst comprising mesostructured material comprising silicon and element

Performing dehydration and simultaneous skeletal isomerization of a load comprising monohydric alcohol containing 4C and 0.5-50% of water to produce olefinic hydrocarbons having 4C at a temperature of 250-550[deg] C, under a pressure of 0.1-1 MPa and at a space velocity of 0.1-10 hours -> 1>, comprises utilizing a catalyst comprising a mesostructured material comprising silicon (Si) and an element (X) consisting of aluminum, boron, gallium, indium and germanium.

METHOD FOR DEHYDRATING ETHYLENE ETHYLENE WITH LOW ENERGY CONSUMPTION

PROCESS FOR THE TREATMENT OF C4 HYDROCARBONS COMPRISING BUTADIENE AND ACETYLENIC COMPOUNDS COMPRISING STAGES OF DISTILLATION AND SELECTIVE HYDROGENATION

On décrit un procédé de traitement d'une charge à 4 atomes de carbone qui contient des composés diéniques et une mineure partie de composés acétyléniques. On soutire latéralement (7) une partie du fluide circulant dans une zone (2) de distillation qui est enrichie en composés acétyléniques, de préférence dans la zone d'épuisement, on réalise une étape d'hydrogénation sélective dans une zone (8) d'hydrogénation externe à la zone de distillation. L'effluent (12) d'hydrogénation produit est recyclé dans la zone de rectification. On récupère en tête (3) une coupe C4 comportant le butadiène et appauvrie en composés acétyléniques et en fond (13) une coupe C5 enrichie en oligomères. A method of treating a 4 carbon feed which contains diene compounds and a minor portion of acetylenic compounds is described. A portion of the fluid circulating in a distillation zone (2) which is enriched in acetylenic compounds, preferably in the exhaustion zone, is laterally withdrawn (7), a selective hydrogenation step is carried out in a zone (8) d hydrogenation external to the distillation zone. The hydrogenation effluent (12) produced is recycled to the rectification zone. A C4 cut comprising butadiene and depleted in acetylenic compounds is recovered at the top (3) and at the bottom (13) a C5 cut enriched in oligomers.

Preparing propylene and a desulfurized gasoline with high octane index comprises selective hydrogenation of gasoline producing flow in separation unit to give light and heavy fractions and separating the obtained fractions

Production of propylene and coproduction of a desulfurized gasoline of high octane index made of a charge having 4-5 carbon atom fraction (I) resulting from a steam-cracking unit and a fluid catalytic cracked gasoline (FCC) unit comprises selective hydrogenation of the FCC to give an effluent that is sent into a separation unit (21) to give a light fraction sent into an oligocracking unit (40), and a heavy fraction sent into a water-treatment unit (30) and separating the obtained fractions in a distillation columns (50) in to at least 5 fractions e.g. a propylene fraction. Production of propylene and coproduction of a desulfurized gasoline of high-octane index made of a charge containing 4-5 carbon atom fraction (I) resulting from a steam-cracking unit (A) and a fluid catalytic cracked gasoline (FCC) unit. The process comprises selective hydrogenation of FCC producing an effluent, which is sent into a separation unit (21) to give a light fraction sent into an oligocracking unit (40), and a heavy fraction containing more than 6 carbon atoms is sent into a water-treatment unit (30) and separating the obtained fractions in a distillation columns (50) into at least 5 fractions like: a fraction mainly made up of ethylene; a fraction of propylene; an intermediate fraction having a 4 carbon molecule in which a part is recycled at the entry of the oligocracking unit, and a non-recycled part is upgraded in liquefied petroleum gas; an intermediate fraction mainly made up of 5-6 carbon atom molecule in which a part is recycled at the entry of the oligocracking unit; and a non recycled part having gasoline directed towards the gasoline pool and a basic fraction of 9 carbon atom molecule sent in to the water-treatment unit in which an effluent from the water-treatment unit having the desulfurized gasoline.

METHOD FOR DEHYDRATING A MIXTURE CONTAINING ETHANOL AND ISOPROPANOL

L'invention se rapporte à un procédé de production d'un mélange d'éthylène et de propylène à partir d'un mélange contenant de l'éthanol, de l'isopropanol et ayant une teneur en eau comprise entre 30 et 75% poids par rapport au poids total du mélange, dans lequel: a) on met en contact dans une unité de déshydratation le mélange avec un catalyseur de déshydratation choisi parmi: • une alumine (A) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 200 et 350 m /g, un diamètre moyen mésoporeux compris entre 5 et 15 nm, une teneur en sodium inférieure à 50 ppm poids et une teneur en soufre inférieure à 40 ppm poids; et • une alumine (B) ayant une surface spécifique BET mesurée selon la norme ASTM D 3663-03 comprise entre 130 et 180 m /g, un diamètre moyen mésoporeux compris entre 14 et 20 nm, une teneur en sodium comprise entre 300 et 600 ppm poids et une teneur en soufre comprise entre 800 et 1300 ppm poids; la mise en contact étant effectuée à une température comprise entre 350 et 500°C, à une pression totale comprise entre 0,2 et 2 MPa et avec une vitesse pondérale horaire (pph) définie comme étant le rapport du débit massique en éthanol et isopropanol sur la masse de catalyseur comprise entre 1 et 10 h-1, b) on soutire un effluent contenant de l'éthylène et du propylène de ladite unité de déshydratation.

PROCESS FOR THE PREPARATION OF ALCOHOLIC ESTERS FROM TRIGLYCERIDES AND ALCOHOLS USING HETEROGENEOUS CATALYSTS ASSOCIATING AT LEAST ONE SOLUTION OF ZNXAI203 + XETDU ZNO TYPE

PROCESS FOR PRODUCING ETHYLENE OXIDE FROM A THERMO-MECHANICALLY INTEGRATED ETHANOL FLOW

L'invention concerne un procédé de déshydratation d'une charge éthanol en éthylène puis d'oxydation de l'éthylène en oxyde d'éthylène comprenant une étape de vaporisation d'une charge comprenant ladite charge éthanol et au moins une partie d'un flux d'eau de dilution comprenant de l'éthanol recyclé de manière à produire une charge vaporisée, une étape de compression dans un compresseur entraîné par une turbine à condensation entraînée par la vapeur générée par l'étape d'oxydation, une étape de déshydratation d'un mélange comprenant ladite charge vaporisée comprimée, une étape de séparation de l'effluent issu de l'étape de déshydratation en un effluent comprenant de l'éthylène et un effluent comprenant de l'eau, une étape de purification d'au moins une partie de l'effluent comprenant de l'eau et la séparation en au moins un flux d'eau traitée et un flux d'eau de dilution comprenant de l'éthanol, ce dernier étant recyclé en amont de l'étape de vaporisation, et une étape d'oxydation de l'éthylène compris dans l'effluent comprenant de l'éthylène en oxyde d'éthylène, cette étape d'oxydation comprenant au moins un réacteur tubulaire d'oxydation refroidi par vaporisation d'un flux de trempe, ledit flux de trempe vaporisé permettant l'entraînement d'une turbine à condensation. The invention relates to a process for the dehydration of an ethanol feedstock to ethylene and then to the oxidation of ethylene to ethylene oxide comprising a step of vaporizing a feedstock comprising said feedstock ethanol and at least a part of a feedstock. dilution water comprising ethanol recycled to produce a vaporized charge, a compression step in a compressor driven by a condensation turbine driven by the vapor generated by the oxidation step, a dehydration step of a mixture comprising said compressed vaporized charge, a step of separating the effluent from the ...

PROCESS FOR THE DIRECT CONVERSION OF A CHARGE COMPRISING FOUR AND / OR FIVE ATOMIC CARBON OLEFINS FOR THE PRODUCTION OF PROPYLENE WITH CO-PRODUCTION OF GASOLINE

PROCESS FOR SEPARATING NON-LINEAR OLEFINS FROM AN OLEFINIC FILLER BY REACTIVE DISTILLATION

La présente invention concerne un procédé de traitement par distillation réactive d'une charge oléfinique comprenant des oléfines linéaires à n atome de carbone, et des oléfines ramifiées, les oléfines ramifiées comprenant des oléfines ramifiées tertiaires, par exemple un mélange de n-butènes et d oléfines ramifiées tertiaires comprenant l'isobutène, de manière à produire un effluent oléfinique avec une teneur massique en oléfine ramifiée tertiaires inférieure ou égale à 3% poids et un effluent hydrocarbures lourds, ledit procédé comprenant l'alimentation d'une section de distillation réactive en ladite charge oléfinique et en une charge alcool comprenant un alcool primaire, ladite section de distillation réactive comprenant une colonne composée au moins d'une zone supérieure de reflux dans laquelle est introduit ladite charge alcool, comprenant par exemple de l'éthanol, une zone intermédiaire réactionnelle comprenant au moins 6 doublets réactifs et une zone inférieure de fractionnement au niveau de laquelle ladite section est alimentée en ladite charge oléfinique, ladite section de distillation réactive étant opérée à une pression relative comprise entre 0,3 et 0,5 MPa, une température en tête de colonne comprise entre 40°C et 60°C, avec un taux de reflux compris entre 1,8 et 2,2. The present invention relates to a process for the reactive distillation treatment of an olefinic charge comprising linear olefins containing n carbon atoms and branched olefins, the branched olefins comprising tertiary branched olefins, for example a mixture of n-butenes and d tertiary branched olefins comprising isobutene, so as to produce an olefinic effluent with a mass content of tertiary branched olefin less than or equal to 3% by weight and a heavy hydrocarbon effluent, said process comprising feeding a reactive distillation section with said olefinic charge and an alcohol charge comprising a primary alcohol, said reactive distillation section comprising a ...

PROCESS FOR PRODUCING TERTIARY OLEFIN BY DECOMPOSITION OF TERTIARY ALKYL ETHER

PROCESS FOR THE DEHYDRATION AND ISOMERIZATION OF C4 ALCOHOLS USING AN AMORPHOUS SOLID WITH ADAPTED POROSITY

La présente invention a pour objet un procédé de production d'oléfines en C4, à partir d'une charge de monoalcool en C4 dans lequel on réalise une réaction de déshydratation du monoalcool en au moins une oléfine, et une réaction d'isomérisation squelettale d'au moins une des oléfines produites dans une même enceinte réactionnelle, en présence d'un catalyseur à base d'alumine à porosité adaptée. The subject of the present invention is a process for producing C4 olefins from a C4 monoalcohol feedstock in which a monohydric alcohol dehydration reaction is carried out in at least one olefin, and a skeletal isomerization reaction is carried out. at least one of the olefins produced in the same reaction chamber, in the presence of an alumina catalyst with a suitable porosity.

PROCESS FOR PRODUCING PROPYLENE OPERATING IN A MOVING BED WITH RECYCLING OF A CATALYST FRACTION USING THE SAME

L'invention consiste en un procédé permettant de produire du propylène à partir d'une coupe légère oléfinique de vapocraquage et/ou de craquage catalytique, ce procédé comprenant une étape de craquage catalytique en lit mobile avec une boucle de régénération du catalyseur.Le procédé réalise le recyclage d'une partie du catalyseur usé à l'entrée du réacteur fonctionnant en lit mobile.L'invention permet d'obtenir une conversion élevée avec un bon rendement et une bonne sélectivité en propylène. The invention consists of a process for producing propylene from a light olefinic fraction of steam cracking and / or catalytic cracking, this process comprising a step of catalytic cracking in a moving bed with a catalyst regeneration loop. recycles part of the spent catalyst at the inlet of the reactor operating as a moving bed. The invention makes it possible to obtain a high conversion with a good yield and a good selectivity for propylene.