EP0949317B1 - Procédé f d'isomérisation d'essences à teneur élevée en benzène - Google Patents
Procédé f d'isomérisation d'essences à teneur élevée en benzène Download PDFInfo
- Publication number
- EP0949317B1 EP0949317B1 EP99400568A EP99400568A EP0949317B1 EP 0949317 B1 EP0949317 B1 EP 0949317B1 EP 99400568 A EP99400568 A EP 99400568A EP 99400568 A EP99400568 A EP 99400568A EP 0949317 B1 EP0949317 B1 EP 0949317B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluid
- reactor
- make
- process according
- isomerization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Definitions
- the present invention relates to an improved method for the isomerization of gasoline with a high benzene content.
- gasoline isomerization processes which aim to increase the octane number of these species by transformation of linear paraffins which contain branched paraffins (or isoparaffins).
- the load to be treated is mainly composed of saturated hydrocarbons with five or six carbon atoms, as well as lower proportions of hydrocarbons to four or seven carbon atoms, and benzene which like everyone knows is relatively difficult to separate from other hydrocarbons with six carbon atoms.
- the charge to be treated is most often mixed with hydrogen and to a possible recycle, then directed to at least one reactor containing a suitable catalyst in a fixed bed.
- the temperature prevailing in this reactor is usually between 120 and 190 ° C.
- effluents are routed to one or more separation columns. Often times isoparaffins are then separated from non-paraffins isomerized: the first are sent in principle to the essences pool, to serve as bases for the formulation of fuels, while the seconds are eventually recycled to the reactor, to be transformed there.
- the first reactor in which product, in addition to the isomerization of paraffins, the hydrogenation of traces of benzene present in the load, operates at slightly higher temperature than the second, where the isomerization reaction ends proper. Indeed, from a kinetic point of view, the paraffin isomerization reaction is slower than the benzene hydrogenation reaction. In addition, the lower temperature prevailing in the second reactor is thermodynamically favorable for product formation branched trees sought.
- the benzene content of the fillers isomerization remains relatively limited. Indeed, a commonly accepted rule considers that an increase in the benzene content of 1% in the feed to be treated a 10 ° C rise in temperature within the first isomerization reactor. Knowing that other reactions that the hydrogenation of benzene already produce to them only a temperature rise of around 15 ° C, the benzene content of the feedstock entering this reactor must then be limited to 4%. Beyond this content, the temperature in the reactor is too high, which ultimately damages not only the catalyst but also the unit, designed to operate at room temperature limited. Furthermore, at high temperature, reactions unwanted side effects occur, such as, by example, hydrocracking reactions of the charge.
- An ingenious solution then consists in admitting in the isomerization unit, in addition to the conventional charges, cuts of benzene-rich gasolines, such as some fuel cuts from reforming units or catalytic cracking: the benzene present in these cuts is thus hydrogenated in the isomerization unit, and this ultimately reduces the content of benzene of the said cuts before sending them to the "pool essences ", term by which we designate all the bases used to make petroleum products.
- the patent US N ° 5,003,118 proposes to introduce, upstream of the isomerization reactors themselves, a charge pretreatment, specifically intended for perform the hydrogenation of the benzene present in this charge. In this way, the unit is able to deal with fillers with higher benzene content.
- This solution has the disadvantage of being of high cost, linked to the necessary construction of additional equipment. Besides, it is absolutely not flexible, insofar as the hydrogenation reactor is of no useful in the case of a load with a low benzene content.
- the present invention therefore aims to propose a method isomerization of gasoline with a high benzene content, allowing a simple and inexpensive remedy to problems encountered in the prior art.
- the present invention also aims to provide a particularly flexible isomerization process, allowing to adapt quickly to different charges intended for him.
- the subject of the present invention is a process for the isomerization of a hydrocarbon feed containing a substantial amount of paraffinic hydrocarbons with 5 or 6 carbon atoms and of benzene at a content greater than or equal to 2% by weight, in which the charge to be treated passes, in the presence of hydrogen, to a total pressure greater than or equal to 10 ⁇ 10 5 Pa (10 bars) and to an average temperature between 100 and 200 ° C., in at least one reactor containing a catalyst of isomerization of paraffinic hydrocarbons, this process being characterized in that one introduces, in the upstream part of the reaction zone, a make-up fluid which, at 40 ° C and under atmospheric pressure (1.0134.10 5 Pa ), is in the gaseous state and has a density less than or equal to that of normal-pentane considered under the same conditions, this make-up fluid comprising at least 98% by weight of hydrocarbons comprising from one to four ato carbon.
- density of a gaseous fluid is meant the ratio between the density of this fluid and the density dry air with normal carbon dioxide content, these two densities being measured in the same temperature and pressure conditions.
- the density of the make-up fluid will be measured, at 40 ° C and under a pressure of 1.0134.10 5 Pa (1 atmosphere), by applying to any of the fluids any of the standardized measurement methods described in standard ASTM D1070-85 (R94). The same is true for normal-pentane.
- the densities of said makeup fluid and of pentane will be considered by reference to the same measurement method.
- the makeup fluid is in the gaseous state at 40 ° C under a pressure of 1.0134.10 5 Pa (1 atmosphere).
- it is introduced into the upstream part of the reaction zone under conditions of temperature and pressure directly dependent on the operating conditions of the process. Depending on its composition, it can then be in the liquid or gaseous state or in an intermediate state.
- the preferred hydrocarbons in the make-up fluid are methane and ethane.
- This fluid can thus, for example, be made of natural gas.
- This fluid can also comprise, in quantity minority, hydrocarbons with six or seven atoms of carbon, and / or inert gases such as nitrogen, or any other suitable light fluid.
- said makeup fluid contains a substantial amount of light compounds from a fractionation column located downstream of the isomerization unit.
- This drop in temperature therefore depends only on the following parameters: flow rates and load compositions and make-up fluid, pressure, temperature, fraction vaporized charge at the reactor inlet and report mass between hydrogen and charge in the mixture reaction allowed in the unit. So it can be perfectly controlled and optimized according to the benzene content of the feed to be isomerized.
- the process according to the invention is precise and extremely flexible, since the flow of the makeup fluid can be adjusted to compensate exactly the temperature rise due to the content of benzene higher than the generally accepted maximum level.
- the method according to the invention proves to be very advantageous for units which do not have, downstream of the isomerization unit, a deisohexanizer (column of separation of the branched paraffins sought and the linear paraffins), with recycle of a cut rich in linear paraffins upstream of the isomerization unit.
- One of the goals of this recycling is to dilute the fresh load allowed in the unit, in order to lower the benzene content. Thanks to the invention, since it is it is possible to admit more content to the unit high in benzene, this dilution is no longer necessary.
- the method according to the invention therefore represents a very valid alternative to the costly installation of a deisohexanizer and a system of recycle.
- the process according to the invention has been found to provide increased recovery light hydrocarbons containing not more than four atoms of carbon, and in particular propane and butane.
- LPG Petroleum Gas Liquefied
- the isomerization unit can be so operated with a view to increased production of these LPGs.
- the make-up fluid is injected into the upstream part of the reaction zone. This means that said fluid can be injected into the part upstream of the first reactor proper, and / or immediately upstream of the latter.
- make-up fluid is injected in the upstream part of the first isomerization reactor, at know in the area extending from the level of introduction into the reaction mixture reactor (feed and hydrogen) halfway up the catalytic bed.
- Make-up fluid can then be injected into the reactor area included between the introduction of the reaction mixture and the start of the dense bed of catalyst.
- fluid can also be injected directly into the dense bed of catalyst, in the first half of this latest.
- make-up fluid When make-up fluid is injected immediately in upstream of the first reactor, it is introduced immediately before the introduction of the reaction mixture (charge and hydrogen) in the first reactor, i.e. after complete preheating of this mixture and before injection of this in the first reactor.
- This injection of makeup fluid has a purely thermal and therefore has nothing to do with the injection, in large quantities, of the hydrogen necessary for the actual isomerization reaction, which takes place, in a manner known per se, upstream of the unit isomerization, i.e. upstream of the heat exchangers heat in which the reaction mixture (charge and hydrogen) is heated before being introduced into the reactor.
- make-up fluid is therefore carried out, moreover, compared to the usual injection of hydrogen in upstream of the unit, in a completely different location, and with a much lower volume flow.
- this make-up fluid which has a purely thermal effect, can consist of any gas light compatible with the process, while hydrogen introduced upstream of the isomerization unit has an effect chemical at the level of the actual reaction.
- This make-up fluid is advantageously injected at a rate of 5 to 150 Nm 3 per m 3 of charge to be isomerized and, preferably, from 5 to 60 Nm 3 per m 3 of charge.
- the starting charge is considered here, before mixing with hydrogen and heating of the reaction mixture thus obtained.
- the make-up fluid either injected at a temperature below or above that of the reaction medium. That said, it is better inject said fluid at a lower temperature or equal to that of the reaction medium and, preferably, between 20 and 180 ° C.
- a particularly variant advantageous of the invention consists in recycling, immediately downstream of the first reactor, a rich section into slightly branched paraffins with 5 or 6 carbon atoms and which usually contains naphthenes. This cut comes, in a manner known per se, from a fractionation existing in advanced isomerization units, which is located downstream of the reactors, and which separates the isoparaffins sought from other compounds.
- this recycle cut which does not contains no benzene, is traditionally introduced upstream of the first reactor, in order not only to perform an additional passage in the isomerization unit, but also to dilute the fresh charge allowed in the unit, to so as to lower the benzene content of the charge combined thus obtained.
- a make-up fluid supply line can open in the finish line at the first reactor of the mixture reaction (charge and hydrogen), between the warming up the most downstream reaction mixture and injection point of said mixture in the first reactor.
- the make-up fluid When the make-up fluid is introduced into the breast of the first reactor, at least one means of introducing make-up fluid flows into this reactor, upstream of the bed dense catalyst and / or within the first half of this last.
- the one or more means can then be constituted by any known means allowing, downstream of the injection of the charge itself, the introduction of a light fluid in a reactor.
- a cane or even a single tube with side slits or more orifices, to allow better distribution of the make-up fluid.
- a diffuser is used allowing to introduce the make-up fluid so homogeneous over the entire section of the reactor.
- said means for introducing make-up fluid can lead into the reactor in multiple ways.
- said means open out transversely in the reactor, substantially perpendicular to the axis of the latter.
- At least one means of introduction of make-up fluid opens into the reactor substantially parallel to the axis of the latter.
- said means then enters the reactor by the orifice allowing the introduction of the reaction mixture.
- the invention does not relate to catalysts capable of to intervene in its implementation.
- We can, in fact, employ any known catalyst exhibiting activity for isomerization of linear paraffins into paraffins branched.
- many catalysts are known to those skilled in the art. They usually have a or more acidic functions, as well as a function hydrogenating (hydrogenating transition metal).
- FIG. 1 represents a unit for the isomerization of sections containing linear paraffins with 5 or 6 atoms of carbon.
- This charge arrives via line 1, in which hydrogen and possibly recycle gases are introduced by line 2.
- the reaction mixture thus obtained is routed by line 33 to two heat exchangers heat 3 and 4, against the effluent from both unit isomerization reactors.
- the reaction mixture thus reheated is then introduced into a first reactor 5, or upstream reactor.
- the latter contains a isomerization catalyst distributed in a catalytic bed 6, which occupies most of the height of the reactor 5.
- the effluent from the latter, after passing through the exchanger 4 is then introduced via line 7 into the second reactor 8, or downstream reactor, which is also loaded with an isomerization catalyst distributed in a catalytic bed 9.
- the load to be treated flows from high down in reactors 5 and 8, but it could naturally circulate there from bottom to top.
- the device further includes valve systems, not represented, allowing to interrupt independently feeding reactors 5 and 8 and / or reversing the direction circulation of the reaction mixture.
- a make-up fluid is injected into the upstream reactor 5, via a rod 11 substantially perpendicular to the axis of the reactor and which leads directly into the catalytic bed, into the first half of it.
- This rod is provided with side slits, not shown, allowing better distribution.
- the catalytic bed 6 of the upstream reactor 5 can be separated into an upstream section 12 and a downstream section 13, which contain the same isomerization catalyst.
- the rod 11 a for introducing make-up fluid then enters the reactor between the two catalytic sections 12 and 13.
- a stepped injection system 11b allows the introduction of make-up fluid at several levels in the first half of the catalytic bed 6 of the reactor 5.
- an injection system 11 c of make-up fluid opens into the reactor 5 in a manner substantially parallel to the axis of the latter, at the orifice allowing the introduction of the reaction mixture (feed and hydrogen) supplied to the reactor via line 33.
- a line 11 d for supplying make-up fluid opens into the inlet line 33 of the reaction mixture (feed and hydrogen), immediately upstream of the first reactor. isomerization 5.
- FIG. 6 shows how the invention can allow improve the relationships between the unit isomerization and other petroleum units.
- the fraction rich in isopentane which is a compound with high octane number therefore requiring no treatment isomerization, is evacuated via line 19.
- Light petrol depleted in isopentane then crosses the two reactors isomerization 5 and 8 as described above, and the load enriched in isoparaffins is extracted therefrom by line 10.
- This charge is then separated, within the stabilizer 20, in a head section 21, consisting of compounds with up to four carbon atoms, and a cut background 22 of heavier compounds .: The latter is then directed to the deisohexanizer 23, where it found divided into an isomerate 26, consisting of isoparaffins with 5 or 6 carbon atoms, and a heavy cut 25, essentially consisting of naphthenes and paraffins at 7 carbon atoms or more.
- the essence heavy discharged from separator 15 via line 17 is directed towards the reforming unit 27, within which it undergoes among others aromatization reactions, which contribute to increase its content of aromatic products, including benzene.
- the reformate thus produced is then separated at level of fractionation 28 into a heavy reformate 29, the boiling point is above about 90 ° C, which is routed to the gasoline pool, and a light reformate 31, whose boiling point is between about 30 ° C and 90 ° C.
- a means 11 for injecting a make-up fluid enters the catalytic bed of the upstream reactor 5.
- the make-up fluid consists of compounds comprising at most 4 carbon atoms derived from the line 35 of the head cup, discharged at 21, from stabilizer 20.
- the isomerization unit is likely to deal with charges with content higher in benzene than in the prior art. So the Doubling the amount of benzene present in the charge can be thermally compensated by adding fluid light (density less than or equal to that of normal-pentane), the flow rate of which will be adjusted according to the benzene content of the feed to be isomerized.
- the purpose of this example is to illustrate the limits of conventional gasoline isomerization processes, in the case treatment of loads with high benzene content.
- This charge is combined with a gaseous mixture rich in hydrogen (20% by weight of hydrogen), introduced at a flow rate of 2 t / h.
- This reaction mixture is then warmed up to 133 ° C., then treated in a conventional gasoline isomerization unit comprising two reactors in series, operating at a pressure of 31 ⁇ 10 5 Pa.
- the temperature recorded at the outlet of the first reactor is 180 ° C.
- this charge No. 2 has a content of benzene of 7.66% by weight and a density at 15 ° C of 0.687. The other properties remain globally unchanged by in relation to charge # 1.
- This charge n ° 2 is treated under the same conditions than those mentioned above for the treatment of charge # 1, except gas flow rich in hydrogen, which is brought to 3.5 t / h (so known per se, the isomerization of charges rich in benzene requires an increased amount of hydrogen in the medium reactive, taking into account the additional consumption hydrogen induced by the hydrogenation of benzene).
- the temperature recorded at the outlet of the first reactor is then 193 ° C. So there was an increase in temperature of 13 ° C in this reactor, due to the high quantity of heat given off by the hydrogenation of the supplement benzene present in charge # 2. Ultimately, this temperature increase in the first reactor risk not only damage the catalyst and the unit, but also to decrease the reaction yields isomerization (better at low temperature).
- charge rich in benzene described above (charge n ° 2) is treated this time according to the isomerization process according to the invention.
- a fluid make-up is therefore introduced into the catalytic bed of the first reactor, at the level of the first third of the bed catalytic (exactly 2/7 of this bed), and with a flow of 30Nm3 per m3 of load.
- Two introduction temperatures make-up fluid have been tested: 30 ° C (temperature lower than that of the reaction medium) and 145 ° C. (temperature of the order of that of the reaction medium).
- Fluid Composition (in% by weight) Density (40 ° C, 1.0134 Pa) F1 2% H 2 + 12% CH 4 + 18% C 2 H 6 + 25% C 3 H 8 + 43% C 4 H 10 1.04.10 -3 F2 2% H 2 + 80% CH 4 + 16% C 2 H 6 + 2% C 3 H 3 0.59.10 -3 F4 100% CH 4 0.62.10 -3 F5 100% C 2 H 6 1.16.10 -3 F6 100% C 3 H 8 1.72.10 -3 F7 100% nC 4 H 10 2.28.10 -3
- the fluid F1 corresponds to a gaseous mixture of the type of those that can recover at the head of a column of fractionation located downstream of the isomerization unit (so-called stabilization column).
- the operating conditions are identical to those described in Example 1 for the treatment of the charge n ° 2, and the inlet temperature of the reaction mixture in the first isomerization reactor is notably maintained at 133 ° C.
- Test 1 corresponds to a zero makeup fluid flow rate (prior art).
- Trial Fluid flow extra (Nm 3 per m 3 of charge)
- Temperature release of the first reactor (° C) 1 0 193 2 10 188 3 30 181 4 60 173
- This example illustrates the excellent thermal control to which the invention gives access.
- This control is extremely precise and flexible, since the fluid flow can be optimized according to the characteristics the load to be treated and, in particular, its content benzene.
- This example specifies the conditions in which the process according to the invention must be implemented work, and in particular the nature of the make-up fluids likely to be employed.
- thermodynamic effect described is not produces more and the injection of make-up fluid does not allow more to lower the temperature of the first reactor.
- the thermodynamic effect described is not produces more and the injection of make-up fluid does not allow more to lower the temperature of the first reactor.
Description
- la figure 1 est une vue schématique d'une unité d'isomérisation incluant une injection d'un fluide d'appoint, conformément à l'invention; .
- les figures 2, 3, 4, 5 sont des variantes de réalisation de la figure 1;
- la figure 6 est une vue synoptique illustrant les relations d'une unité d'isomérisation avec d'autres unités pétrolières, telles qu'elles existent dans l'art antérieur, d'une part, et telles que modifiées conformément à l'invention, d'autre part.
- point 5% (en volume) de distillation A.S.T.M.: 31°C,
- point 95% (en volume) de distillation A.S.T.M : 86°C,
- teneur en soufre: 1 ppm en poids,
- teneur en azote: 1 ppm en poids,
- teneur en benzène: 3,5% en poids,
- densité à 15°C: 0,680.
Fluide | Composition (en % en poids) | Densité (40°C, 1,0134 Pa) |
F1 | 2 % H2 + 12 % CH4 + 18 % C2H6 + 25 % C3H8 + 43 % C4H10 | 1,04.10-3 |
F2 | 2 % H2 + 80 % CH4 + 16 % C2H6 +2 % C3H3 | 0,59.10-3 |
F4 | 100 % CH4 | 0,62.10-3 |
F5 | 100 % C2H6 | 1,16.10-3 |
F6 | 100 % C3H8 | 1,72.10-3 |
F7 | 100 % nC4H10 | 2,28.10-3 |
Fluide d'appoint | Température de sortie du premier réacteur | |
F1 | 180 °C | 183 °C |
F2 | 180 °C | 181 °C |
F4 | 179 °C | 180 °C |
F5 | 180 °C | 182°C |
F6 | 179 °C | 184 °C |
F7 | 181 °C | 187 °C |
Essai | Débit du fluide d'appoint (Nm3 par m3 de charge) | Température de sortie du premier réacteur (°C) |
1 | 0 | 193 |
2 | 10 | 188 |
3 | 30 | 181 |
4 | 60 | 173 |
- F1 et F5 sont les fluides déjà mentionnés dans l'Exemple 2 et correspondent aux conditions de l'invention : fluides gazeux à 40°C, sous une pression de 1,0134.105 Pa (1 atmosphère) et de densité inférieure à celle du pentane considéré dans les mêmes conditions.
- F9 et F10 sont des fluides plus lourds que le pentane.
Fluide | Composition | Etat physique (densité) à 40°C, 1,0134.105Pa | Température sortie 1er réacteur (°C) |
F1 | Mélange (H2, C1 à C4) | gazeux (1,04.10-3) | 183 |
F5 | 100% C2H3 | gazeux (1,16.10-3) | 182 |
F9 | 100% nC6H14 | liquide | 192 |
F10 | 100% nC9H20 | liquide | 196 |
Claims (16)
- Procédé d'isomérisation d'une charge hydrocarbonée contenant une quantité substantielle d'hydrocarbures paraffiniques à 5 ou 6 atomes de carbone et du benzène à une teneur supérieure ou égale à 2 % en pois, dans lequel la charge à traiter passe, en présence d'hydrogène, à une pression totale supérieure ou égale à 10.105 Pa (10 bars) et à une température moyenne comprise entre 100 et 200°C, dans au moins un réacteur (5) contenant un catalyseur d'isomérisation d'hydrocarbures paraffiniques, ce procédé étant caractérisé en ce que l'on introduit, dans la partie amont de la zone réactionnelle, un fluide d'appoint qui, à 40°C et sous pression atmosphérique (1, 0134.105 Pa), se trouve à l'état gazeux et possède une densité inférieure ou égale à celle du normal-pentane considéré dans les même conditions, ce fluide d'appoint contenant au moins 98 % en poids d'hydrocarbures comportant de un à quatre atomes de carbone.
- Procédé selon la revendication 1, caractérisé en ce que les hydrocarbures comportant de un à quatre atomes de carbone sont issus d'une colonne de fractionnement (20) des effluents de l'unité d'isomérisation.
- Procédé selon l'une quelconque des revendications 1 et 2, caractérisé en ce que ledit fluide d'appoint comprend également des hydrocarbures à six ou sept atomes de carbone, et/ou des gaz inertes tels que de l'azote, ou tout autre fluide léger approprié.
- Procédé selon l'une des revendications 1 à 3, caractérisé en ce que du fluide d'appoint est injecté dans la partie amont du premier réacteur d'isomérisation (5), à savoir dans la zone s'étendant du niveau d'introduction dans ce réacteur du mélange réactionnel (charge et hydrogène) jusqu'à mi-hauteur du lit catalytique (6).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que du fluide d'appoint est injecté immédiatement en amont du premier réacteur, c'est-à-dire après préchauffage complet du mélange réactionnel (charge et hydrogène) et avant injection dudit mélange dans le premier réacteur (5).
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que ledit fluide d'appoint est injecté à un débit de 5 à 150 Nm3 par m3 de charge.
- Procédé selon la revendication 6, caractérisé en ce que ledit fluide d'appoint est injecté à un débit de 5 à 60 Nm3 par m3 de charge.
- Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que ledit fluide d'appoint est injecté à une température inférieure ou égale à celle du milieu réactionnel et, de préférence, comprise entre 20 et 180°C.
- Procédé selon l'une quelconque des revendications précédentes, dans lequel l'unité d'isomérisation comprend plusieurs réacteurs en série (5, 8), caractérisé en ce qu'une coupe riche en paraffines non isomérisées à 5 ou 6 atomes de carbone et qui contient généralement des naphtènes, provenant de la séparation et du traitement des effluents de l'unité d'isomérisation, est recyclée immédiatement en aval du premier réacteur (5).
- Procédé selon l'une des revendications 1 à 9, caractérisé en ce que du fluide d'appui est introduit dans la ligne d'alimentation de la zone réactionnelle en mélange réactionnel (charge et hydrogène), entre un moyen de réchauffement (4) de ce mélange et le point d'injection de celui-ci dans la zone réactionnelle (5).
- Procédé selon l'une des revendications 1 à 9, caractérisé en ce que du fluide d'appoint est introduit dans la zone réactionnelle (5) en amont d'un lit dense de catalyseur (6) et/ou au sein de la première moitié de ce lit.
- Procédé selon la revendication 11, caractérisé en ce que, en vue d'assurer une meilleure distribution du fluide d'appoint, celui-ci est introduit au moyen d'une canne ou d'un tube pourvu(e) de fentes latérales ou d'une pluralité d'orifices.
- Procédé selon l'une des revendications 11 et 12, caractérisé en ce que en vue de répartir le fluide d'appoint de façon homogène suivant toute la section de la zone réactionnelle (5), ce fluide est introduit à l'aide d'un diffuseur.
- Procédé selon l'une des revendications 1 à 13, caractérisé en ce que du fluide d'appoint est introduit dans la zone réactionnelle transversalement à l'axe du réacteur (5) sensiblement perpendiculairement à l'axe de ce réacteur.
- Procédé selon l'une des revendications 1 à 13, caractérisé en ce que le fluide d'appoint est introduit dans la zone réactionnelle par l'orifice d'introduction du mélange réactionnel de façon sensiblement parallèle à l'axe du réacteur (5).
- Procédé selon l'une des revendications 1 à 15, dans lequel la zone réactionnelle (5) comprend un lit comportant une section amont (12) et une section aval (13) distinctes, caractérisé en ce que le fluide d'appoint est introduit dans la zone réactionnelle entre les deux sections catalytiques (12) et (13).
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9803958 | 1998-03-31 | ||
FR9803958A FR2776667B1 (fr) | 1998-03-31 | 1998-03-31 | Procede et dispositif d'isomerisation d'essences a teneur elevee en benzene |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0949317A1 EP0949317A1 (fr) | 1999-10-13 |
EP0949317B1 true EP0949317B1 (fr) | 2004-05-19 |
Family
ID=9524679
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP99400568A Expired - Lifetime EP0949317B1 (fr) | 1998-03-31 | 1999-03-09 | Procédé f d'isomérisation d'essences à teneur élevée en benzène |
Country Status (8)
Country | Link |
---|---|
US (2) | US6416657B1 (fr) |
EP (1) | EP0949317B1 (fr) |
JP (1) | JP4112114B2 (fr) |
AT (1) | ATE267239T1 (fr) |
DE (1) | DE69917363T2 (fr) |
ES (1) | ES2221327T3 (fr) |
FR (1) | FR2776667B1 (fr) |
ZA (1) | ZA992450B (fr) |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6573417B1 (en) * | 2001-11-05 | 2003-06-03 | Uop Llc | Fractionation of paraffin isomerization process effluent |
US8517185B2 (en) * | 2008-10-08 | 2013-08-27 | Cummins Filtration Ip, Inc. | Two stage fuel water separator and particulate filter utilizing pleated nanofiber filter material |
US8590712B2 (en) * | 2008-10-08 | 2013-11-26 | Cummins Filtration Ip Inc. | Modular filter elements for use in a filter-in-filter cartridge |
FR2943070B1 (fr) | 2009-03-12 | 2012-12-21 | Total Raffinage Marketing | Fluide hydrocarbone hydrodeparaffine utilise dans la fabrication de fluides industriels, agricoles ou a usage domestique |
FR2943064B1 (fr) | 2009-03-12 | 2013-12-06 | Total Raffinage Marketing | Diluant hydrocarbone a bas taux de cov pour materiaux de construction |
CN102596862B (zh) * | 2009-05-15 | 2015-09-30 | 康明斯过滤Ip公司 | 表面聚结器 |
US8692046B2 (en) | 2011-01-13 | 2014-04-08 | Uop Llc | Process for isomerizing a feed stream including one or more C4-C6 hydrocarbons |
US8716544B2 (en) | 2011-01-13 | 2014-05-06 | Uop Llc | Process for isomerizing a feed stream including one or more C4-C6 hydrocarbons |
US10058808B2 (en) | 2012-10-22 | 2018-08-28 | Cummins Filtration Ip, Inc. | Composite filter media utilizing bicomponent fibers |
FR3015514B1 (fr) | 2013-12-23 | 2016-10-28 | Total Marketing Services | Procede ameliore de desaromatisation de coupes petrolieres |
CN109475790A (zh) | 2016-07-19 | 2019-03-15 | 康明斯滤清系统知识产权公司 | 穿孔层聚结器 |
CN110320307A (zh) * | 2019-08-02 | 2019-10-11 | 中国科学院新疆理化技术研究所 | 一种可控制安石榴苷异构体比例的低温进样方法 |
Family Cites Families (24)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2393041A (en) * | 1944-05-08 | 1946-01-15 | Shell Dev | Process for the isomerization of paraffin hydrocarbons |
US2920033A (en) * | 1955-05-02 | 1960-01-05 | Texaco Inc | Hydrocarbon conversion process with the recycling of an enriched hydrogen stream |
US3359198A (en) * | 1965-07-09 | 1967-12-19 | Universal Oil Prod Co | Gas purification method |
US3674681A (en) * | 1970-05-25 | 1972-07-04 | Exxon Research Engineering Co | Process for isomerizing hydrocarbons by use of high pressures |
US3755144A (en) * | 1971-10-13 | 1973-08-28 | Universal Oil Prod Co | Hydrocarbon isomerization and separation process |
US3864240A (en) * | 1973-03-09 | 1975-02-04 | Universal Oil Prod Co | Integration of a reaction system having gravity-flowing catalyst particles with a fixed-bed system |
US4058452A (en) * | 1976-07-19 | 1977-11-15 | Uop Inc. | Alkylaromatic hydrocarbon dealkylation process |
US4333818A (en) * | 1981-01-26 | 1982-06-08 | Uop Inc. | Separation of normally gaseous hydrocarbons from a catalytic reforming effluent and recovery of purified hydrogen |
US4432862A (en) * | 1982-01-18 | 1984-02-21 | Exxon Research And Engineering Co. | Reforming and isomerization process |
US4747933A (en) * | 1987-03-27 | 1988-05-31 | Uop Inc. | Isomerization unit with integrated feed and product separation facilities |
FR2623203B1 (fr) * | 1987-11-17 | 1990-03-16 | Inst Francais Du Petrole | Amelioration de l'echange thermique charge/effluent d'une unite de traitement d'hydrocarbures sous hydrogene par recyclage partiel de produit |
US5648590A (en) * | 1989-07-10 | 1997-07-15 | Sun Company, Inc. (R&M) | Liquid phase isomerization of alkanes |
US5003118A (en) * | 1989-12-29 | 1991-03-26 | Uop | Isomerization of benzene-containing feedstocks |
GB2242910A (en) * | 1990-04-11 | 1991-10-16 | Shell Int Research | Process for the isomerization of a hydrocarbon feed |
GB9013565D0 (en) * | 1990-06-18 | 1990-08-08 | Shell Int Research | Process for producing gasoline components |
US5245102A (en) * | 1990-11-29 | 1993-09-14 | Uop | Isomerization with distillation and psa recycle streams |
US5146037A (en) * | 1990-11-29 | 1992-09-08 | Uop | Isomerization with distillation and psa recycle streams |
US5227554A (en) * | 1991-11-29 | 1993-07-13 | Mobil Oil Corporation | Isomerization process |
DE69326030T2 (de) * | 1992-01-15 | 2000-01-05 | Inst Francais Du Petrole | Erniedrigung des Benzolgehaltes von Benzinen |
US5360534A (en) * | 1993-05-24 | 1994-11-01 | Uop | Isomerization of split-feed benzene-containing paraffinic feedstocks |
FR2714388B1 (fr) * | 1993-12-29 | 1996-02-02 | Inst Francais Du Petrole | Procédé de réduction de la teneur en benzène dans les essences. |
US5516964A (en) * | 1994-01-21 | 1996-05-14 | Sun Company, Inc. (R&M) | Hydrocarbon isomerization using solid superacid catalysts comprising platinum metal |
FR2715931B1 (fr) * | 1994-02-08 | 1996-04-26 | Total Raffinage Distribution | Procédé d'isomérisation de n-paraffines en isoparaffines. |
US5830345A (en) * | 1996-02-28 | 1998-11-03 | Chinese Petroleum Corporation | Process of producing a debenzenated and isomerized gasoline blending stock by using a dual functional catalyst |
-
1998
- 1998-03-31 FR FR9803958A patent/FR2776667B1/fr not_active Expired - Fee Related
-
1999
- 1999-03-09 ES ES99400568T patent/ES2221327T3/es not_active Expired - Lifetime
- 1999-03-09 DE DE69917363T patent/DE69917363T2/de not_active Expired - Fee Related
- 1999-03-09 AT AT99400568T patent/ATE267239T1/de not_active IP Right Cessation
- 1999-03-09 EP EP99400568A patent/EP0949317B1/fr not_active Expired - Lifetime
- 1999-03-30 ZA ZA9902450A patent/ZA992450B/xx unknown
- 1999-03-31 US US09/282,442 patent/US6416657B1/en not_active Expired - Fee Related
- 1999-03-31 JP JP09214899A patent/JP4112114B2/ja not_active Expired - Fee Related
-
2002
- 2002-03-28 US US10/107,477 patent/US6881385B2/en not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
JP4112114B2 (ja) | 2008-07-02 |
ATE267239T1 (de) | 2004-06-15 |
US6881385B2 (en) | 2005-04-19 |
DE69917363T2 (de) | 2005-05-12 |
US6416657B1 (en) | 2002-07-09 |
ES2221327T3 (es) | 2004-12-16 |
JPH11323356A (ja) | 1999-11-26 |
DE69917363D1 (de) | 2004-06-24 |
ZA992450B (en) | 1999-10-01 |
FR2776667B1 (fr) | 2000-06-16 |
EP0949317A1 (fr) | 1999-10-13 |
US20020139712A1 (en) | 2002-10-03 |
FR2776667A1 (fr) | 1999-10-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0949317B1 (fr) | Procédé f d'isomérisation d'essences à teneur élevée en benzène | |
EP0922750B1 (fr) | Essences à haut indice d'octane et leur production par un procédé associant hydro-isomérisation et séparation | |
EP2333031B1 (fr) | Procédé de production de carburants kérosène et diesel de haute qualité et de coproduction d'hydrogène à partir de coupes saturées légères | |
EP0922748B1 (fr) | Procédé de séparation d'une charge C5-C8 ou d'une charge intermédiaire, en trois effluents respectivement riches en paraffines linéaires, monobranchées et multibranchées | |
WO2003057802A2 (fr) | Vapocraquage de naphta modifie | |
EP1167491A1 (fr) | Procédé pour l'hydrogénation de coupes contenant des hydrocarbures | |
CA2730515C (fr) | Procede d'hydrogenation du benzene | |
JP6100785B2 (ja) | 燃料および燃料ブレンドを製造するためのシステムおよびプロセス | |
EP1640436B1 (fr) | Procédé d'isomérisation d'une coupe C7 avec coproduction d'une coupe cycliques riche en méthylcyclohexane | |
WO2016102302A1 (fr) | Procede et dispositif pour la reduction des composes aromatiques polycycliques lourds dans les unites d'hydrocraquage | |
EP1088879A1 (fr) | Procédé de production d'essences à indice d'octane amélioré | |
CA2665197A1 (fr) | Traitement pour enlever au moins du benzene des courants d'hydrocarbure | |
EP1281669A1 (fr) | Procédé de récuperation d'hydrogène dans un effluent hydrocarboné gazeux, avec mise en oeuvre d'un réacteur membranaire | |
FR2852323A1 (fr) | Nouveau procede de reformage regeneratif | |
EP3087160B1 (fr) | Procede ameliore de desaromatisation de coupes petrolieres | |
EP0934996A1 (fr) | Procédé de séparation chromatographique d'une charge C5-C8 ou d'une charge intermédiaire en trois effluents, respectivement riches en paraffines linéaires, monobranchées et multibranchées | |
EP0949316A1 (fr) | Procédé de conversion d'hydrocarbures par traitement dans une zone de distillation associée à une zone réactionnelle et son utilisation en hydrogénation du benzène | |
FR3081166A1 (fr) | Procédé de séparation des n paraffines et des isoparaffines d’une huile d’hydrocarbures | |
FR2787117A1 (fr) | Procede de conversion d'hydrocarbures par traitement dans une zone de distillation associee a une zone reactionnelle comprenant le recontactage du distillat vapeur avec la charge, et son utilisation en hydrogenation du benzene | |
EP1508609B1 (fr) | Procédé de traitement d'une fraction intermédiaire issue d'effluents de vapocraquage | |
EP1496099A1 (fr) | Procédé amélioré d'isomérisation d'une coupe C7 avec ouverture des cycles naphténiques | |
FR2474524A1 (fr) | Procede de conversion des hydrocarbures | |
WO2017009109A1 (fr) | Procede permettant de realiser le bouclage du bilan thermique sur une unite de craquage catalytique de naphta dite ncc | |
Klimov et al. | Manufacture of motor fuels on IK-30-BIMT catalyst | |
FR2820754A1 (fr) | Dispositif comprenant un recyclage vers un separateur, et en melange avec une charge, de l'effluent liquide issu d'un absorbeur |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU NL PT SE |
|
AX | Request for extension of the european patent |
Free format text: AL;LT;LV;MK;RO;SI |
|
17P | Request for examination filed |
Effective date: 19991001 |
|
AKX | Designation fees paid |
Free format text: AT BE CH DE DK ES FI FR GB GR IE IT LI LU NL PT SE |
|
17Q | First examination report despatched |
Effective date: 20030311 |
|
GRAP | Despatch of communication of intention to grant a patent |
Free format text: ORIGINAL CODE: EPIDOSNIGR1 |
|
RTI1 | Title (correction) |
Free format text: PROCESS FOR THE ISOMERISATION OF GASOLINES WITH HIGH BENZENE CONTENT |
|
GRAS | Grant fee paid |
Free format text: ORIGINAL CODE: EPIDOSNIGR3 |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: TOTALFINAELF FRANCE |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU NL PT SE |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IE Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040519 Ref country code: FI Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040519 Ref country code: AT Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040519 |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: FG4D Free format text: NOT ENGLISH |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: EP |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FG4D Free format text: FRENCH |
|
REF | Corresponds to: |
Ref document number: 69917363 Country of ref document: DE Date of ref document: 20040624 Kind code of ref document: P |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SE Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040819 Ref country code: GR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040819 Ref country code: DK Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 20040819 |
|
GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) |
Effective date: 20040826 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2221327 Country of ref document: ES Kind code of ref document: T3 |
|
REG | Reference to a national code |
Ref country code: IE Ref legal event code: FD4D |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LU Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20050309 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LI Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20050331 Ref country code: CH Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20050331 |
|
26N | No opposition filed |
Effective date: 20050222 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: PL |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: PT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20041019 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: FR Payment date: 20070328 Year of fee payment: 9 Ref country code: ES Payment date: 20080328 Year of fee payment: 10 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: NL Payment date: 20080318 Year of fee payment: 10 Ref country code: IT Payment date: 20080326 Year of fee payment: 10 Ref country code: GB Payment date: 20080320 Year of fee payment: 10 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20080321 Year of fee payment: 10 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: BE Payment date: 20080430 Year of fee payment: 10 |
|
BERE | Be: lapsed |
Owner name: *TOTALFINAELF FRANCE Effective date: 20090331 |
|
GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 20090309 |
|
NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee |
Effective date: 20091001 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST Effective date: 20091130 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20091001 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090331 Ref country code: NL Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20091001 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090309 Ref country code: FR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20091123 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20090310 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: ES Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090310 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090309 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20090331 |