EP1370630A1 - Procede de production d'une essence desulfuree a partir d'une coupe essence contenant de l'essence de craquage - Google Patents
Procede de production d'une essence desulfuree a partir d'une coupe essence contenant de l'essence de craquageInfo
- Publication number
- EP1370630A1 EP1370630A1 EP02701343A EP02701343A EP1370630A1 EP 1370630 A1 EP1370630 A1 EP 1370630A1 EP 02701343 A EP02701343 A EP 02701343A EP 02701343 A EP02701343 A EP 02701343A EP 1370630 A1 EP1370630 A1 EP 1370630A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- gasoline
- sulfur
- compounds
- catalyst
- olefins
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
-
- 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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
-
- 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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/06—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a selective hydrogenation of the diolefins
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/08—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including acid treatment as the refining step in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
-
- 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 invention relates to a diagram for the desulfurization of conversion essences and in particular of essences from catalytic cracking, catalytic cracking in a fluid bed (FCC), a coking process (coking in the language of Shakespeare), a visbreaking process (visbreaking in the language of Shakespeare), a pyrolysis process.
- This process can also treat direct distillation essences (straight run in English) mixed with at least one of the essences mentioned above.
- the process of the present invention makes it possible to achieve high desulfurization rates by limiting the loss of octane due to the saturation of the olefins observed during the hydrodesulfurization reactions.
- the invention relates to a process for the production of gasoline with a low sulfur content comprising a hydrogenation, a step of transformation of the sulfur compounds, a step of alkylation of the sulfur compounds not transformed in the preceding step, a fractionation into a light fraction. and in at least one heavy fraction and optionally one or more intermediate fractions, and a hydrodesulfurization of a heavy fraction and / or of an intermediate fraction.
- This process makes it possible to enhance a gasoline cut possibly comprising also hydrocarbons with two three or four carbon atoms, by reducing the total sulfur content of said cut to very low levels compatible with current or future specifications.
- This desulphurization is also carried out without appreciable reduction in the gasoline yield and while minimizing the reduction in the octane number
- the units for hydrotreating catalytic cracking feedstocks operate under severe temperature and pressure conditions, which supposes a significant consumption of hydrogen and a high investment.
- the entire charge must be desulphurized, which entails the treatment of very large charge volumes.
- the gasolines to be treated generally have an initial point greater than 70 ° C., and again it is necessary to treat the light gasoline separately (fraction corresponding to the compounds with a boiling point comprised between the C5 hydrocarbons at 5 carbon atoms and 70 ° C) for example by means of a softening.
- the process for desulfurization of a naphtha cut comprising an olefinic gasoline comprises a step of weighing down the sulfur-containing compounds by alkylation followed by a step of fractionating the gasoline into two cuts, the gasoline slight being depleted in sulfur.
- the process for producing desulfurized gasoline comprises a separation of the gasoline into a light gasoline and a heavy gasoline.
- the light petrol is sent to a reactor for weighing down sulfur-containing compounds by alkylation.
- the heavy petrol additive with reactive olefins is sent to a reactor for weighing down sulfur compounds by alkylation.
- the heavy gasoline and the light gasoline are mixed then sent to a distillation which makes it possible to recover, at the head, a gasoline depleted in sulfur.
- the gasoline to be desulfurized is treated in a process comprising a step ai) of selective hydrogenation of the diolefinic compounds, optionally at least one step a2) aimed at increasing the molecular weight of the light sulfur products present in the initial gasoline to be desulphurized, at least one step b) of separation of the gasoline obtained at the end of step ai) and / or a2) into two separate sections, one of which is a section light practically free of sulfur and containing the lightest olefins of the initial gasoline and the other heavy cut containing the major part of the sulfur compounds present in the initial gasoline and / or the sulfur compounds resulting from step a2), at least one step c) of processing the heavy cut making it possible to break down or to hydrogenate the unsaturated sulfur compounds present in this cut and in particular the cyclic or even aromatic sulfur compounds under conditions of limited hydrogenation of the olefins present in this cut and at least one step
- the present invention makes it possible to produce a desulfurized gasoline while limiting the loss of octane by desulfurization.
- the scheme of the present invention differs from conventional desulfurization schemes which are based on desulfurization of the total gasoline. In some cases these diagrams provide for a separation of the gasoline into at least two cups: a cup containing the light gasoline and a cup containing the heavy gasoline, that is to say a gasoline with a final boiling point greater than that of light petrol.
- Heavy gasoline is desulfurized for example by hydrogen treatment or by absorption of sulfur compounds.
- the schemes including a hydrogen treatment lead to a significant saturation of the olefins, and consequently, to a high loss of octane
- the light gasoline that can be desulfurized under mild conditions by hydrodesulphurization, washing with a basic solution or adsorption on solid or softened by an oxidation process such as for example the Merox process ® from Universal Oil Products (UOP) which can be extractive.
- an oxidation process such as for example the Merox process ® from Universal Oil Products (UOP) which can be extractive.
- Certain diagrams make it possible to desulfurize only heavy petrol, the sulfur compounds usually present in light petrol (mercaptans) having been previously weighed upstream of a distillation or fractionation zone (splitter in the language of Shakespeare).
- mercaptans light petrol
- fractionation zone splitter in the language of Shakespeare.
- the processes for weighing down sulfur-containing compounds by alkylation presented above they make it possible to produce a light desulfurized gasoline, the heavy gasoline concentrating the heavy sulfur-containing compounds and weighed down by alkylation. These methods therefore do not make it possible to desulfurize the entire conversion gasoline fraction and in particular that obtained from catalytic cracking units.
- the processes for weighing down sulfur-containing compounds by alkylation are based on acid catalysis. The lifetime of the catalyst can be limited by the presence of diolefins and basic compounds (mainly nitrogen) in the gasoline to be treated.
- the present invention relates to a process for producing essences with a low sulfur content, which makes it possible to recover the whole of a petrol cut containing sulfur, preferably a petrol cut of catalytic cracking or of coking (coking according to English terminology). , or pyrolysis, or viscoreduction (visbreaking according to English terminology), possibly mixed with a direct distillation gasoline, and reduce the sulfur contents in said gasoline cut to very low levels, without appreciable reduction in gasoline yield while minimizing the decrease in the octane number due to the hydrogenation of olefins.
- the feedstock of the process according to the invention may also optionally comprise, in addition to a gasoline cut, a C4 " cut comprising hydrocarbons with two, three or four carbon atoms.
- the present invention relates to a process for producing low sulfur gasolines from an initial gasoline containing at least 150 parts per million by weight (ppm), often at least 200 ppm and most often at least 300 ppm of sulfur compounds comprising at least the following stages:
- step b) aiming at increasing the molecular weight of light sulfur products mainly of those which are in the form of mercaptans having from 1 to 6 carbon atoms in their molecules and of sulfides often having from 2 to 6 carbon atoms in their molecules initially present in the gasoline introduced in step a) and / or those contained in the product resulting from step a),
- the term "mainly” means that during the step concerned at least 50% of the sulfur-containing compounds which are in the form of the compounds of the indicated type are converted.
- stage e) is a stage of treatment of at least one of the heavier fractions separated in stage d) on a catalyst making it possible to decompose at least partially the sulfur-containing compounds carried out under conditions where the hydrogenation of olefins on this catalyst is limited.
- the treatment of at least one of the heavier fractions resulting from stage d) and preferably heavy gasoline is carried out in two stages:
- step e) of treatment of at least one of the heavier fractions and preferably of the heavy gasoline separated in step d) on a catalyst making it possible to at least partially decompose the sulfur-containing compounds, in conditions where the hydrogenation of olefins on this catalyst is limited
- polyunsaturated compounds covers diolefinic hydrocarbon compounds that is to say containing two double bonds, hydrocarbon compounds containing more than two double bonds but non-aromatic and hydrocarbon compounds containing at least one triple bond present in the original essence. Most often the initial essence contains as polyunsaturated compounds essentially diolefinic compounds.
- the gasoline with a low sulfur content that is obtained is a gasoline containing less than 150 ppm by weight, often less than 100 ppm and most often less than 80 ppm by weight of sulfur.
- Stage b) of transformation of the light sulfur compounds usually relates essentially to the transformation of the saturated sulfur compounds having a boiling point below 120 ° C.
- This step can optionally be carried out simultaneously with step a) on all or part of the initial gasoline, in the same reactor or in a different reactor. It can also be carried out separately on all or part of the hydrogenated gasoline in step a).
- this step b) the thiophene and the thiophenic compounds are little transformed.
- this step a) of hydrogenation of the unsaturated compounds and step b) aiming to increase the molecular weight of the light saturated sulfur products initially present in the gasoline introduced in step a) are optionally carried out simultaneously in a single reaction zone containing one or more beds of a single catalyst.
- Step c) is an alkylation step of the sulfur compounds usually belonging to the group comprising the thiophene, the thiophene compounds and the mercaptans present in the product resulting from step b).
- the mercaptans possibly present are either those formed in step a) and / or b), or those present in the initial gasoline and not converted in step a) and / or b).
- This step can be carried out in one or more reactors in series or in parallel.
- the first reactor can act as a guard bed intended to retain the basic compounds possibly present in the starting gasoline.
- These basic compounds can also be at least partially removed before the introduction of the gasoline in step a) of hydrogenation of the polyunsaturated compounds.
- This elimination is preferably carried out by treatment with an acidic aqueous solution.
- the operating conditions can be adjusted so that a part of the olefins of the starting gasoline is converted into long branched olefins by addition reactions between olefins. Likewise, the operating conditions can be adjusted so that some of the aromatics are weighed down by alkylation with olefins.
- Step d) of fractionation of the gasoline obtained at the end of step c) comprises the fractionation into at least two fractions (or cuts), a light fraction preferably practically free of sulfur and containing the most olefins light of the initial gasoline (light gasoline or light fraction), and a heavy fraction in which preferably the major part of the sulfur compounds initially present in the initial gasoline and / or formed during stages a), b) and c ) is concentrated (petrol or heavy fraction). It is also possible to separate the gasoline obtained in step c) in addition to two fractions, that is to say for example a light fraction, at least an intermediate fraction and a heavy fraction. In this case, the intermediate fraction (s) can be sent to a catalytic reforming unit usually after a thorough desulfurization step.
- Step e) for treating heavy gasoline and / or an intermediate fraction containing a proportion of sulfur compounds very much greater than that contained in the light fraction is a step for treating this fraction on a catalyst making it possible to decompose at least partially the sulfur compounds, in particular the cyclic or even aromatic sulfur compounds such as for example the thiophenic compounds, by placing themselves in conditions where the hydrogenation of olefins on this catalyst is limited.
- Stage f) is a stage of treatment of the product obtained in stage e), without elimination of I ⁇ 2S formed during this stage e), on a catalyst and under conditions making it possible to decompose or at least partially hydrogenate the sulfur compounds not transformed during step e), and preferably to decompose or hydrogenate the unsaturated sulfur compounds and the linear and / or cyclic saturated sulfur compounds that are not transformed during step e) and in particular the thiophenic compounds and mercaptans, with limited hydrogenation of olefins.
- Steps e) and f) are most often carried out in at least two successive and distinct reaction zones.
- the catalytic treatments carried out during steps e) and f) can be carried out either in a single reactor containing the two catalysts, or in at least two different reactors.
- the latter two are placed in series, the second reactor preferably treating all of the effluent leaving the first reactor, preferably without separation of the liquid and the gas between the first and the second reactor. It is also possible to use several reactors in parallel or in series for one and / or the other of steps e) and / or f).
- step f it is not necessary to remove the H2S formed during step e) before sending the effluent from this step e) to the inlet of the hydrodesulfurization reactor (s). step f).
- One of the advantages of the process according to the invention therefore lies in the fact that it is not necessary to adjust the H2S content between step e) and step f).
- a step g) is preferably carried out after step f), this step consists in mixing the light gasoline separated in step d) and at least part of the heavy gasoline resulting from step f) to form the desired global desulfurized gasoline.
- all of the heavy gasoline desulfurized from step f) is mixed with the light gasoline from step d), without separation of the liquid and the gas contained in the heavy gasoline after desulfurization, optionally a simple stripping with at least one inert gas can be carried out to remove I ⁇ 2S from heavy gasoline which is largely desulphurized, that is to say usually containing less than 50% by weight and often less than 20% by weight of residual sulfur compounds by with respect to the content of sulfur compounds in the heavy petrol leaving step d).
- step g the recovery of light petrol and desulfurized heavy petrol is carried out separately. It is then unnecessary to carry out step g).
- the charge of the process according to the invention is a gasoline cutter containing sulfur, preferably a gasoline cutter coming from a cracking unit most often from a catalytic cracking unit, the range of boiling points of which extends typically from about the boiling points of hydrocarbons with 2 or 3 carbon atoms (C2 or C3) to about 250 ° C, preferably from about the boiling points of hydrocarbons with 2 or 3 carbon atoms (C2 or C3) up to about 220 ° C, more preferably from about the boiling points of 5 carbon atoms (C5) hydrocarbons to about 220 ° C.
- the process of the present invention applies more particularly to catalytic cracked gasolines whose final boiling temperatures are from approximately 120 ° C. to approximately 230 ° C.
- the operating conditions can be adjusted in order to favor the alkylation reactions of the olefins with the olefins and the aromatics, which causes, in particular, a drop in the vapor pressure of the gasoline.
- At least one fraction resulting from the fractionation stage preferably the heavy fraction or an intermediate fraction, can be treated in a stage of transformation of these sulfur-containing compounds into H2S (hydrogen sulfide) with or without minimizing the saturation of the olefins.
- the heavy gasoline or at least one intermediate fraction is treated in a hydrodesulfurization section, preferably in the presence of a hydrodesulfurization catalyst or optionally an absorbent.
- a hydrodesulfurization catalyst or optionally an absorbent Preferably, no desulfurization of the light fraction is necessary in the process according to the invention, since most of the sulfur compounds initially present in gasoline are found in the heavy fraction and possibly in the intermediate fraction (s) of l step d) of fractionation which is carried out after the steps of hydrogenation, of transformation of the sulfur-containing compounds (step b), of transformation of the thiophenic compounds and optionally mercaptans, in particular residual mercaptans which are not converted and / or formed in steps a) and b) (step c) by alkylation of at least part of the sulfur compounds not converted in step b) (step c).
- This sequence makes it possible to ultimately obtain a desulfurized gasoline without significant reduction in the olefin content or in the octane number, even for high desulfurization rates, and this without it being necessary to treat the gasoline. light by means of a hydrodesulfurization or softening section, or by having recourse to processes making it possible to restore the octane number of the gasoline. Thanks to this process, significant desulfurization rates are reached, under reasonable operating conditions specified below.
- the sulfur species contained in the feeds treated by the process of the invention can be mercaptans, sulfides, disulfides and / or heterocyclic compounds, such as for example thiophene or alkyl-thiophenes, or heavier compounds, such as for example benzothiophene and / or dibenzothiophene.
- the petrol fractionation point is preferably limited in order to avoid the presence of sulfur compounds in light petrol. In the absence of the sulfur compounds alkylation reactor, it would be possible to separate in light gasoline only the C5 olefins and a small part of the C6 olefins under penalty of causing an excessively large fraction of thiophene in this cut.
- the method according to the invention is advantageous by carrying out a step for transforming thiophene and more generally thiophenic compounds, for example by means of an alkylation section upstream of the fractionation section or integrated into said section according to a mode detailed in the following description.
- step b) To make it possible to recover a larger fraction of the light petrol while limiting the sulfur content of this fraction without additional treatment, it is preferably proposed to treat the feed in step b) under conditions and on catalysts which make it possible to transform the light sulfur compounds present in the form of mercaptans and sulphides most often having from 2 to 6 carbon atoms in their molecule into sulfur compounds of higher boiling point found after separation, possibly in at least an intermediate fraction or in heavy petrol. These intermediate and / or heavy cuts can then be desulfurized.
- This desulphurization is carried out under defined conditions and by means of a hydrodesulphurization catalyst which optionally makes it possible to limit the saturation of the olefins or according to a preferred embodiment of the invention, by means of a chain of catalysts making it possible to reach levels high desulfurization while limiting the rate of hydrogenation of olefins and therefore the loss of octane.
- a hydrodesulphurization catalyst which optionally makes it possible to limit the saturation of the olefins or according to a preferred embodiment of the invention, by means of a chain of catalysts making it possible to reach levels high desulfurization while limiting the rate of hydrogenation of olefins and therefore the loss of octane.
- the sulfur content of gasoline cuts produced by catalytic cracking and in particular of catalytic cracking in a fluid bed (FCC) depends on the sulfur content of the feed treated with the FCC, on the presence or not of a pretreatment of the feed of the FCC, as well as the end point of the cut.
- the sulfur contents of an entire gasoline cut, in particular those originating from the FCC are greater than 150 ppm by weight and most of the time greater than 500 ppm by weight.
- the sulfur contents are often greater than 1000 ppm by weight, they can even in certain cases reach values of the order of 4000 to 5000 ppm by weight.
- the process according to the invention applies in particular when high rates of desulphurization of petrol are required, that is to say when the desulphurized petrol must contain at most 10% of the sulfur of the initial petrol and possibly at most 5% or more 2% of the sulfur in the initial gasoline, which corresponds to desulfurization rates higher than 90% or even higher than 95 or 98%.
- the process according to the invention comprises at least the following stages a) to e): Stage a) of selective hydrogenation of the diolefins: this stage is intended to eliminate the diolefins which are capable of causing premature deactivation of the catalysts d weighing down the sulfur-containing compounds by alkylation during step c) below, and to form gums in the desulfurized gasolines.
- This step is carried out by passing the charge, preferably consisting of the entire gasoline cutter, over a catalyst making it possible to selectively hydrogenate the diolefins of the gasoline without hydrogenating the olefins.
- Step b) weighing down the light mercaptans and sulphides on a catalyst based on a supported metal: this reaction can be carried out in the selective hydrogenation reactor for diolefins.
- This step consists in passing all or part of the initial gasoline or of the hydrogenated gasoline in step a), preferably all of the initial or hydrogenated gasoline in step a), over a catalyst making it possible to transform at least partially the light sulfur compounds (for example: ethylmercaptan, propyl mercaptan), by reaction with all or part of the olefins, into heavier sulfur compounds.
- the light sulfur compounds for example: ethylmercaptan, propyl mercaptan
- This step is for example carried out simultaneously with step a) by passing, for example, the initial gasoline over a catalyst capable of both hydrogenating the diolefins and of transforming the light sulfur compounds, preferably with the olefins, into sulfur compounds heavier, or on a separate catalyst but allowing this transformation to be carried out in the same reactor as that used for carrying out step a)
- Step c) is a step of weighing down the sulfur-containing compounds by alkylation. This step makes it possible to remove most of the sulfur compounds present in the form of thiophenics by an addition reaction on the olefins.
- This stage consists in passing all or part of the gasoline resulting from stage b) on a catalyst having an acid function which makes it possible to carry out the addition of the sulfur-containing compounds in the form of mercaptans and sulphides on the olefins and the reaction of alkylation of thiophene and thiophene derivatives by these same olefins.
- Step d) of fractionation of the gasoline obtained at the end of step c) is intended to produce a light desulfurized gasoline at the top of the distillation column.
- the gasoline thus recovered is poor in sulfur and most often does not require additional treatment.
- This light, low-sulfur petrol is most often sent directly to the petrol storage area (petrol pool according to the terminology most frequently used in the trade) from preferably without additional post treatment.
- the gasoline recovered at the bottom of the column concentrates the sulfur compounds initially present in the feed. This column can include lateral withdrawals making it possible, for example, to obtain one or more intermediate fractions.
- step e) the bottom gasoline and / or that contained in an intermediate fraction from step d) is desulphurized by hydrotreatment.
- the gasoline at the bottom of the column and / or that contained in an intermediate fraction resulting from stage d) is desulphurized in stage e) on a catalyst and under conditions such as saturation of the olefins is partial in order to limit the loss of octane.
- the column bottom gasoline and / or that contained in an intermediate fraction resulting from step d) is desulphurized by hydrotreatment according to a process which limits the saturation of olefins.
- a selective hydrodesulfurization makes it possible to limit the saturation of the olefins and thus limit the loss of octane in the gasoline.
- the heavy gasoline and / or at least one intermediate gasoline thus desulphurized can then be optionally stripped (that is to say that a gas stream, preferably containing one or more inert gases is passed through this gasoline), in order to eliminate ⁇ H 2 S possibly produced during the desulfurization.
- reaction section with the fractionation column.
- Said reaction section (s) then operate on at least one fraction taken from inside the fractionation column and the effluent from the reaction section is returned to the fractionation column.
- the reaction section or sections thus coupled to the fractionation column of step d) can be chosen from the group consisting of the reaction sections of the following steps:
- Such devices comprising a fractionation column associated with an external reactor and which can be used in the process according to the invention have for example been described for applications in the field of refining and petrochemistry in US Patents 5,1777,283, US 5,817,227 and US 5,888,355
- a reactive column in place of the fractionation column, that is to say to place at least one of said reaction sections in the column of fractionation (reaction section internal to the column), preferably in an area where the concentration of reagent is maximum.
- the reaction section will preferably be placed in an area having the maximum concentration of these compounds.
- the reaction section internal to the column is chosen from the group consisting of the following reaction sections: transformation of sulfur compounds such as thiophene, thiophene compounds and optionally mercaptans by alkylation (step c)), desulfurization of the intermediate fractions and / or desulfurization of the heavy fraction ((step e) and / or step f).
- the reaction section is placed in the middle of the fractionation column, so as to treat the compounds having the intermediate boiling points, that is to say the compounds which can constitute a intermediate cut and which are recovered alone or with the heavy fraction at the bottom of the column, at the end of the fractionation step.
- the heavy fraction is then treated in an external reactor associated or not with the fractionation column.
- Another variant of the process according to the invention consists both in using a reactive column comprising at least one reaction section and an external reactor coupled or not coupled to said column.
- Such variants are for example described in patent application WO00 / 15319.
- the variants described above are only illustrations of the possible variants of the method according to the invention.
- the process according to the invention can indeed be implemented by combining reaction sections (steps a), b), c), e) or f)) or associated with the fractionation column of step d ), either internal (s) to said column, or external (s) and not coupled (s) to said column in the sense that the effluent from said reaction section (s) is not recycled to the fractionation column.
- One of the advantages of the process according to the invention lies in the fact that it is most often not necessary to desulfurize the light fraction of the gasoline resulting from the fractionation.
- step b) and / or c) makes it possible to considerably reduce the content of sulfur compounds in the light cut and possibly at least one intermediate cut, and generally to recover the essential of these compounds in the heavy fraction, and possibly in the intermediate fraction (s).
- Steps b) and c) are distinguished, inter alia, by the fact that the conversion of thiophenic compounds is generally less than 60% by weight, or even less than 40% by weight in step b), while the conversion is most often greater at 80% by weight, preferably greater than 90% by weight, very preferably greater than 95% by weight in step c).
- Step b) essentially effects the weighting of light mercaptans and sulfides, while step c) essentially performs the weighting of thiophenic compounds.
- the sulfur compound content of the light fraction thus obtained is usually less than 100 ppm, preferably less than 50 ppm, more preferably less than 20 ppm and very preferably less than 10 ppm.
- Another advantage lies in the fact that the residual content of sulfur-containing compounds in the desulfurized petrol by means of the process according to the invention is particularly low, and that the octane number of the petrol is maintained at a high level.
- step a hydrogenation of diolefins
- the hydrogenation of dienes is a step which makes it possible to eliminate, before hydrodesulfurization, almost all of the dienes present in the gasoline cut containing sulfur to be treated. It preferably takes place in the first step (step a) of the process according to the invention, generally in the presence of a catalyst comprising at least one metal from group VIII, preferably chosen from the group consisting of platinum, palladium and nickel. , and a support.
- a catalyst comprising at least one metal from group VIII, preferably chosen from the group consisting of platinum, palladium and nickel.
- a support a catalyst based on nickel or on palladium deposited on an inert support will be used, such as for example alumina, silica or a support containing at least 50% of alumina.
- the pressure used is sufficient to maintain more than 60%, preferably 80%, and more preferably 95% by weight of the gasoline to be treated in the liquid phase in the reactor; it is most generally between approximately 0.4 and approximately 5 MPa and preferably greater than 1 MPa, more preferably between 1 and 4 MPa.
- the hourly space velocity of the liquid to be treated is between approximately 1 and approximately 20 h ⁇ 1 (volume of charge per volume of catalyst and per hour), preferably between 2 and 10 h "1, very preferably between 3 and 8 h "- .
- the temperature is most generally between about 50 and about 250 ° C, and preferably between 80 and 220 ° C, and more preferably between 100 and 200 ° C, to ensure sufficient conversion of the diolefins. Very preferably it is limited to 180 ° C.
- the hydrogen to charge ratio expressed in liters is generally between 1 and 50 liters per liter, preferably between 2 and 30 liters, more preferably between 3 and 25 liters per liter.
- the choice of operating conditions is particularly important. It will most generally operate under pressure and in the presence of a quantity of hydrogen in slight excess relative to the stoichiometric value necessary for hydrogenating the diolefins.
- the hydrogen and the feedstock to be treated are injected in upward or downward streams into a reactor preferably comprising a fixed bed of catalyst.
- Another metal can be combined with the main metal to form a bimetallic catalyst, such as for example molybdenum or tungsten.
- a bimetallic catalyst such as for example molybdenum or tungsten.
- Catalytic cracking gasoline can contain up to a few percent (%) by weight of diolefins. After hydrogenation, the content of diolefins is generally reduced to less than 3000 ppm, even less than 2500 ppm and more preferably less than 1500 ppm. In some cases it can be obtained less than 500 ppm. The content of dienes after selective hydrogenation can even be reduced to less than 250 ppm if necessary.
- the hydrogenation step of the dienes takes place in a catalytic hydrogenation reactor which comprises a catalytic reaction zone traversed by the entire charge and the quantity of hydrogen necessary to effect desired reactions.
- a catalytic hydrogenation reactor which comprises a catalytic reaction zone traversed by the entire charge and the quantity of hydrogen necessary to effect desired reactions.
- This stage consists in transforming the light sulfur compounds. That is to say the compounds which, at the end of step a) of hydrogenation of the dienes, would be found (after fractionation in step d)) in light petrol, in heavier sulfur compounds entrained in heavy gasoline.
- the light sulfur compounds are chosen from the families of mercaptans of 1 to 6 carbon atoms and sulfides of 2 to 6 carbon atoms.
- This transformation is preferably carried out on a catalyst comprising at least one element from group VIII of the periodic classification of the elements (Handbook of Chemistry and Physics 45 th edition 1964-1965) (groups 8, 9 and 10 of the new periodic classification).
- the choice of catalyst is made in particular so as to promote the reaction between light mercaptans and olefins, which leads to heavier sulfides or mercaptans.
- Other compounds such as COS or CS2 can optionally also be converted.
- This step can possibly be carried out at the same time as step a).
- a catalyst based on nickel identical or different from the catalyst of stage a such as for example the catalyst recommended in the process of patent US-A-3,691,066, which makes it possible to transform the mercaptans (butylmercaptan) into heavier sulfur compounds (sulfides).
- Another possibility for carrying out this step consists in hydrogenating at least part of the thiophene to thiophane, the boiling point of which is higher than that of thiophene (boiling point 121 ° C).
- This step can be carried out on a catalyst based on nickel, platinum or palladium.
- the temperatures are generally between 100 and 300 ° C and preferably between 150 and 250 ° C.
- the H2 / feed ratio is adjusted between 1 and 20 liters per liter, preferably between 3 and 15 liters per liter, to further promote, if possible, the desired hydrogenation of the thiophenic compounds and minimize the hydrogenation of the olefins present in the feed.
- the space velocity is generally between 1 and 10 h "1 , preferably between 2 and 4 h " 1 and the pressure between 0.5 and 5 MPa, preferably between 1 and 3 MPa.
- This step consists in preferably passing all of the fraction from step b) over a catalyst having an acid function which makes it possible to carry out the addition of the sulfur-containing compounds in the form of mercaptans to the olefins and the alkylation reaction. thiophene and thiophene derivatives by these same olefins.
- the operating conditions are adjusted to carry out the desired transformation with conversion rates of thiophene and / or thiophene compounds, greater than 80% by weight, preferably greater than 90% by weight, very preferably greater than 95% by weight.
- Other compounds such as COS or CS2 can optionally also be converted.
- part of the olefins in the starting gasoline can be converted into long branched olefins, by addition reactions (oligomerization) between olefins, and part of the aromatics made heavier by alkylation with the olefins.
- the essence can be added with a compound known to inhibit the oligomerizing activity of acid catalysts such as alcohols, ethers or water.
- the thiophenic compounds whose boiling point is from approximately 60 ° C. to approximately 160 ° C. will react with conversion rates greater than 80% by weight, preferably greater than 90% by weight, with the olefins to form thiophene alkyls whose boiling point is much higher than that of the starting thiophenic compounds.
- Some or all of the benzene can also be removed by alkylation with olefins.
- This alkylation step is carried out in the presence of an acid catalyst.
- This catalyst can be either a resin, a zeolite, a clay, any functionalized silica or any silico-aluminate having an acidity, or any support grafted with acid functional groups.
- the ratio of the volume of charge injected over the volume of catalyst is between 0.1 and 10 liter / liter / hour and preferably between 0.5 and 4 liter / liter / hour.
- this alkylation step is carried out in the presence of at least one acid catalyst chosen from the group consisting of Bronsted acids (including phosphoric, sulfuric, boric, fluoride acids) supported for example on silica, alumina or silica alumina, silicoaluminates titanosilicates, mixed alumina titanium, clays, resins, mixed oxides obtained by grafting at least one organosoluble or water-soluble organometallic compound (chosen from the group consisting of alkyls. and / or alkoxy.
- at least one acid catalyst chosen from the group consisting of Bronsted acids (including phosphoric, sulfuric, boric, fluoride acids) supported for example on silica, alumina or silica alumina, silicoaluminates titanosilicates, mixed alumina titanium, clays, resins, mixed oxides obtained by grafting at least one organosoluble or water-soluble organometallic compound (chosen from the group consisting of alkyls. and
- metals of at least one element such as titanium, silicon zirconium, germanium, tin, tantalum, niobium ...) on at least one oxide such as alumina (gamma, delta, eta forms, alone or as a mixture) silica , alumina silicas, titanium silicas, zirconia silicas or any other solid having any acidity.
- a particular embodiment of the invention may consist in using a physical mixture of at least two of the above catalysts in proportions varying from 95/5 to 5/95, preferably from 85/15 to 15/85 and very preferably from 70/30 to 30/70.
- the temperature for this step is generally from about 10 to about 350 ° C depending on the type of catalyst or the strength of the acidity.
- the temperature is usually from about 50 to about 250 ° C, preferably from about 100 to about 210 ° C.
- the molar ratio of olefins to thiophenic compounds is greater than 10 mole / mole, preferably greater than 100 mole / mole.
- the operating pressure of this step is generally between 0.1 and 3 MPa and preferably such that the charge is in liquid form under the temperature and pressure conditions, ie at a pressure greater than 0.5 MPa.
- step d) The effluent from step c) of transformation of the sulfur-containing compounds is at least partially and preferably entirely sent to a fractionation unit (step d)) to be separated into at least two fractions, a light fraction and a fraction heavy which is preferably sent in full optionally after mixing with an intermediate fraction in a desulfurization zone operating in one (step e) or two successive desulfurization steps (step e) and step f)).
- the essence is divided into two fractions:
- This separation is preferably carried out by means of a conventional distillation column also called a splitter according to the Anglo-Saxon name.
- This fractionation column must make it possible to separate a light fraction of the gasoline containing a small fraction of the sulfur and a heavy fraction preferably containing the major part of the sulfur initially present in the initial gasoline.
- This column generally operates at a pressure between 0.1 and 2 MPa and preferably between 0.2 and 1 MPa.
- the number of theoretical plates of this separation column is generally between 10 and 100 and preferably between 20 and 60.
- the reflux rate expressed as being the ratio of the liquid flow rate in the column divided by the distillate flow rate expressed in kg / h, is generally less than one and preferably less than 0.8.
- the light gasoline obtained at the end of the separation generally consists of hydrocarbon cuts with 5, 6 and 7 carbons.
- this light fraction has a low sulfur content, that is to say that it is not generally necessary to treat the light cut before using it as fuel.
- the essence is preferably divided into at least two cuts having the following properties:
- cut L a so-called light cut (cut L), the boiling points of which are preferably less than approximately 120 ° C.
- This temperature is given as an indication, it generally corresponds to the maximum temperature for which the sulfur content is less than 20 ppm, • at least one so-called heavy cut (cut H1) whose boiling points are above approximately 100 ° C.
- the light section L is preferably injected into a liquid gas separation flask in order to separate the unconsumed hydrogen and the H2S, formed during step a) and or b) and or c), olefins generally having 5 to 7 carbon atoms.
- the so-called heavy section H1 that is to say the section whose temperatures are above about 100 ° C., is sent to the desulphurization zone step e) and preferably steps e) and f).
- the essence is divided into at least 3 fractions: a light fraction, a heavy fraction and at least an intermediate fraction.
- the light fraction is identical to that described above.
- the intermediate fraction 12 whose boiling points by way of example are at least 100 ° C and at most about 140 ° C or even about 160 ° C.
- This cut can be treated in step e) then optionally in step f) of the process according to the invention.
- the heavy fraction H2 is then a fraction whose boiling points are generally greater than about 160 ° C or about 140 ° C. In this case the whole intermediate fraction plus heavy fraction is equivalent to the heavy fraction H1 of the case where the fractionation is limited to two fractions.
- the heavy cut H2 whose boiling temperatures are generally above about 160 ° C or about 140 ° C is sent to the desulphurization zone.
- step c) fractionate the product resulting from step c) in at least three cuts a light cut (L), at least one intermediate cut (12) and at least one heavy cut (H2) having the properties described above.
- the intermediate section 12 the boiling points of which are between approximately 100 ° C. and approximately 120 ° C. or approximately 160 ° C., can be sent to a sulfur compound transformation unit according to step c) or recycled in this step c ).
- the section (s) 12 can again be divided into an intermediate section 13 and a heavy section H3
- the section H3, thus obtained can optionally be mixed with the section H2, preferably before desulfurization and the section 13 can be sent to a sulfur compound processing unit according to step c) or recycled in this step c).
- step e) includes that in which a single desulfurization step is carried out and those of a preferred embodiment of the invention in which the hydrodesulfurization is carried out in two successive steps e) and F).
- step e Decomposition of sulfur compounds from heavy and / or intermediate fractions from step d) (step e):
- This step which applies to heavy gasoline (heavy fractions and / or intermediate fractions) obtained at the end of step d) of fractionation consists in hydrogenolysing at least partially the sulfur-containing compounds to form H 2 S.
- the fraction of sulfur compounds thus transformed depends on the desired degree of desulfurization.
- This step can, for example, be carried out by passing heavy petrol, in the presence of hydrogen, over a catalyst comprising at least one element from group VIII and / or at least one element from group VIB at least partly in sulphide form, at a temperature between about 210 ° C and about 350 ° C, preferably between 220 ° C and 320 ° C, under a pressure generally between about 1 and about 4 MPa, preferably between 1, 5 and 3 MPa.
- the space velocity of the liquid is between approximately 0.5 and approximately 20 h -1 (expressed in volume of liquid per volume of catalyst and per hour), preferably between 0.5 and 10 h -1, very preferably between 1 and 8 h -1
- the H 2 / 1HC ratio is between 100 to 600 liters per liter and preferably between 200 and 500 liters per liter.
- At least one catalyst comprising at least one element from group VIII (metals from groups 8, 9 and 10 of the new classification, i.e. iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium or platinum) and / or at least one element of group VIB (metals of group 6 of the new classification, that is to say chromium, molybdenum or tungsten), on an appropriate support.
- group VIII metal from groups 8, 9 and 10 of the new classification, i.e. iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium or platinum
- group VIB metal of group 6 of the new classification, that is to say chromium, molybdenum or tungsten
- the content of group VIII metal expressed as oxide is generally between 0.5 and 15% by weight, preferably between 1 and 10% by weight.
- the metal content of group VIB is generally between 1.5 and 60% by weight, preferably between 3 and 50% by weight.
- the element of group VIII, when present, is preferably cobalt, and the element of the group Vlb, when it is present, is generally molybdenum or tungsten. Combinations such as cobalt-molybdenum are preferred.
- the catalyst support is usually a porous solid, such as for example an alumina, a silica-alumina or other porous solids, such as for example magnesia, silica or titanium oxide, alone or in combination. mixture with alumina or silica-alumina.
- the catalyst according to the invention preferably has a specific surface of less than 190 m2 / g, more preferably less than 180 m2 / g, and very preferably less than 150 m2 / g.
- the catalyst is preferably used at least in part in its sulfurized form.
- the sulfurization step may be carried out by any technique known to those skilled in the art, in situ or ex situ.
- the conversion of the sulfur compounds is greater than 50% and preferably greater than 90%.
- Step e) is carried out under conditions such that the transformation of at least a portion of the unsaturated sulfur compounds such as the thiophenic compounds, into saturated compounds, for example in thiophanes (or thiacyclopentanes) or in transformation, is observed. mercaptans, or at least partially hydrolyze these unsaturated sulfur compounds to form I ⁇ 2 S.
- the conversion of the unsaturated sulfur compounds is greater than 15% and preferably greater than 50%.
- the hydrogenation rate of the olefins is preferably less than 50%, more preferably less than 40%, and very preferably less than 35%, during this stage.
- the effluent from this first hydrogenolysis step is then sent, preferably without any separation of the liquid and the gas, to step f) which makes it possible to decompose the sulfur-containing compounds saturated in H 2 S.
- the saturated sulfur compounds are transformed in the presence of hydrogen, on a suitable catalyst.
- Decomposition of non-unsaturated compounds hydrogenated in step e) can also take place simultaneously.
- This transformation is carried out without significant hydrogenation of the olefins, that is to say that during this stage the hydrogenation of the olefins is generally limited to 20% by volume relative to the olefin content of the initial gasoline. , and preferably, limited to 10% by volume relative to the olefin content of the initial gasoline.
- the catalysts which may be suitable for this stage of the process according to the invention, without this list being limiting, are catalysts generally comprising at least one basic element chosen from the elements of group VIII and group VIB, and preferably chosen from the group formed by nickel, cobalt, iron, molybdenum, tungsten. These metals can be used alone or in combination, they are preferably supported and used in their sulfurized form.
- the catalyst of step f) is preferably of a different nature and / or composition from that used in step e).
- the base metal content of the catalyst according to the invention is generally between approximately 1 and approximately 60 % by weight, preferably between 5 and 30% by weight, and very preferably between 10 and 25% by weight.
- the catalyst is generally shaped, preferably in the form of beads, pellets, extrudates, for example trilobes.
- the metal can be incorporated into the catalyst by deposition on the preformed support, it can also be mixed with the support before the shaping step.
- the metal is generally introduced in the form of a precursor salt, generally soluble in water, such as for example nitrates, heptamolybdates. This method of introduction is not specific to the invention. Any other method of introduction known to those skilled in the art may be suitable. It is very advantageous to use a catalyst containing at least one element from group VIII and in particular nickel.
- the catalyst supports used in this stage of the process according to the invention are generally porous solids chosen from refractory oxides, such as, for example, aluminas, silicas and silica-aluminas, magnesia, as well as titanium and zinc oxide, the latter oxides can be used alone or as a mixture with alumina or silica-alumina.
- the supports are transition aluminas or silicas whose specific surface is between 25 and 350 m 2 / g. Natural compounds, such as, for example, kieselguhr or kaolin, may also be suitable as supports for the catalysts used in this stage of the process.
- the catalyst is preferably used at least in part in its sulfurized form. This has the advantage of minimizing the risk of hydrogenation of unsaturated compounds such as olefins or aromatic compounds during the phase of start-up.
- the sulfurization step may be carried out by any technique known to those skilled in the art, in situ or ex situ.
- the sulfur content of the catalyst is generally between 0.5 and 25% by weight, preferably between 4 and 20% by weight and very preferably between 4 and 10% by weight.
- the purpose of the hydrodesulfurization carried out during this step is to convert the saturated sulfur compounds of the gasoline which have already undergone at least one prior hydrogenation of the unsaturated sulfur compounds in step e) into 1H 2 S. It makes it possible to obtain an effluent that meets the desired specifications in terms of content of sulfur compounds.
- the gasoline thus obtained has only a small loss of octane.
- the treatment aimed at decomposing the saturated sulfur compounds originating from step e) of the process is carried out in the presence of hydrogen, with the catalyst comprising at least one base metal chosen from the group formed by nickel, cobalt, iron , molybdenum, tungsten, at a temperature between about 280 ° C and about 400 ° C, preferably between about 290 ° C and about 380 ° C, more preferably between 310 ° C and 360 ° C, and very preferably between 320 ° C and 350 ° C, under a pressure generally between about 0.5 and about 5 MPa, preferably between 1 and 3MPa, more preferably between 1, 5 and 3 MPa.
- the space velocity of the liquid is between approximately 0.5 and approximately 10 h ⁇ 1 (expressed in volume of liquid per volume of catalyst and per hour), preferably between 1 and 8 h ⁇ 1 .
- the H 2 / HC ratio is adjusted as a function of the desired hydrodesulfurization rates in the range between approximately 100 and approximately 600 liters per liter, preferably between 100 and 300 liters per liter. All or part of this hydrogen can possibly come from step e) (unconverted hydrogen) or from recycling of the hydrogen not consumed in steps a), b) or c). It has been found that the use of this second catalyst in this step, under specific operating conditions, makes it possible to decompose the saturated compounds, contained in the effluent from step c, into H2S.
- This implementation makes it possible to achieve a high overall level of hydrodesulfurization at the end of all the stages of the process according to the invention, while minimizing the loss of octane resulting from the saturation of the olefins, because the conversion of olefins during step e) is generally limited to at most 20% by volume of the olefins, preferably at most 10% by volume.
- the latter is freed from the major part of its basic nitrogen compounds which are at least partly eliminated before step c) of alkylation d '' at least part of the sulfur compounds present in the product resulting from stage b).
- the basic nitrogen compounds contained in the initial gasoline are at least partially eliminated before its introduction in step a) of hydrogenation of polyunsaturated compounds. Most often the elimination of basic nitrogen compounds is carried out by a treatment (washing) using an acidic aqueous solution.
- the initial gasoline contains basic nitrogen compounds
- these are at least partially removed by a treatment using an acidic aqueous solution carried out before step c) of alkylation of at least part of the sulfur compounds present in the product resulting from stage b).
- This washing is usually carried out before or after the selective hydrogenation treatment in step a) of the polyunsaturated compounds contained in the initial gasoline.
- the catalysts used in steps e) and f) are most often separate sulfur catalysts.
- the gasoline ( ⁇ ) containing sulfur compounds, diolefins and olefins is injected into line (1).
- the hydrogen is injected into line (2) in an amount such that the hydrogen / diolefin molar ratio is greater than 1.
- the gasoline and the hydrogen are brought into contact in a reactor (A) for the selective hydrogenation of diolefins, under conditions optimized to limit the saturation of the olefins while hydrogenating the diolefins.
- the effluent from the reactor (A) is sent via line (3) to a unit for weighing down sulfur compounds (B).
- the reactions implemented in this reactor (B) are essentially reactions of weighting of mercaptans of 1 to 6 carbon atoms as well as sulfides of 2 to 6 carbon atoms. Partial conversion of compounds such as CS2 and COS is also observed.
- the gasoline produced is introduced via line (4) into a reactor (C) for weighing down the sulfur-containing compounds by addition to the olefins.
- the sulfur compounds mainly weighed down in this reactor are the thiophenic compounds.
- oligomerization reactions of olefins and partial alkylation of benzene compounds are therefore both heavier than gasoline ( ⁇ ) and depleted in light sulfur compounds.
- the gasoline produced in the reactor (C) is injected through line (5) into a fractionation column (D) which separates the gasoline in at least two cuts.
- Light gasoline the end point of which can be between 55 ° C and 160 ° C, is recovered at the head of the column. This gasoline is desulphurized and does not require additional treatment. The final temperature of this light gasoline is fixed by the maximum quantity of sulfur authorized.
- the heavy gasoline recovered at the bottom of the column by the line (7) is sent after mixing with hydrogen introduced by the line (8) to a desulfurization section (E + F). This essence has an initial distillation point between 50 ° C and 130 ° C.
- the hydrodesulfurization section (E + F) is designed to desulfurize gasoline while limiting the hydrogenation of olefins, which limits the loss of octane. It consists of at least 2 reactors in series, the first of which (E) includes a catalytic system optimized to saturate the thiophenic compounds and partially transform the sulfur-containing compounds into H2S. The second contains a catalyst which is an optimized catalyst for transforming mercaptans into H2S, by limiting the hydrogenation of olefins present in gasoline.
- This desulfurization scheme was described in patent application EP 1 077 247
- the heavy petrol recovered by the line (10) and the light petrol recovered by the line (6) can be mixed to produce a total desulfurized petrol recovered by the line (11).
- a cracked gasoline is subjected to a diolefin hydrogenation treatment under conditions where the light saturated sulfur compounds present in the feed are partly converted into heavier compounds.
- This treatment is carried out in a reactor operating continuously.
- the catalyst is based on nickel and molybdenum (catalyst sold by the company Procatalyse under the reference HR945).
- the reaction is carried out at 180 ° C. under a total pressure of 2.6 MPa, with a space velocity of 6 h -1 .
- the hV charge ratio, expressed in liters of hydrogen per liter of charge is 10.
- the petrol is separated into two fractions, a light fraction representing 65% by weight of the distilled petrol whose cutting point corresponds to a temperature of 100 ° C. and a heavy fraction.
- the separation is carried out on a discontinuous distillation column composed of 30 theoretical plates. The characteristics of the two fractions obtained are given in Table 2.
- the light fraction has contents of diolefins, mercaptans and sulfur such that it can be used directly, provided that the specification on the sulfur content is greater than 60 ppm.
- Example 1 The catalytic cracking gasoline obtained in Example 1 after the hydrogenation treatment is separated into two fractions, a light fraction representing 20% by weight of the distilled gasoline, the cutting point of which corresponds to a temperature of 55 ° C. and a heavy fraction.
- the separation is carried out on the same column as in Example 1.
- the characteristics of the two fractions obtained are given in Table 3. Table 3
- Light petrol produced by distillation has mercaptan, diolefin and sulfur contents such that it can be used directly.
- Heavy gasoline is therefore subjected to hydrodesulfurization on a chain of catalysts in an isothermal tubular reactor.
- the first catalyst (catalyst A) is obtained by impregnation "without excess solution” of a transition alumina, in the form of beads, with a specific surface of 130 m 2 / g and a pore volume of 0.9 ml / g, with an aqueous solution containing molybdenum and cobalt in the form of ammonium heptamolybdate and cobalt nitrate.
- the catalyst is then dried and calcined in air at 500 ° C.
- the cobalt and molybdenum content of this sample is 3% CoO and 14% MoO3.
- the second catalyst (catalyst B) is prepared from a transition alumina of 140 m 2 / g in the form of beads 2 mm in diameter.
- the porous volume is 1 ml / g of support.
- One kilogram of support is impregnated with 1 liter of nickel nitrate solution.
- the catalyst is then dried at 120 ° C. and calcined under a stream of air at 400 ° C. for one hour.
- the nickel content of the catalyst is 20% by weight.
- 100 ml of catalyst A and 200 ml of catalyst B are placed in two reactors in series, so that the charge to be treated (heavy fraction) first meets catalyst A then catalyst B.
- a sampling zone for the effluent from step e is provided between catalysts A and B.
- the catalysts are first sulfurized by treatment for 4 hours under a pressure of 3.4 MPa at 350 ° C, in contact with a charge containing 2% by weight of sulfur in the form of dimethyldisulfide in
- the temperature of the zone catalytic comprising catalyst A is 280 ° C, the temperature of the catalytic zone containing catalyst B is 330 ° C.
- the desulfurization rate is 92.8%
- the residual sulfur content is 25 ppm
- the loss of octane calculated by the formula (RON + MON) / 2 is 2.75 points.
- the catalytic cracking gasoline obtained in Example 1 after the hydrogenation treatment [steps a) and b) according to the invention] is sent to a reactor for weighing down sulfur compounds by alkylation with olefins (step c) according to the invention).
- the charge is added to isopropanol up to 500 ppm, intended to hydrate the catalyst continuously in the reactor.
- the effluent thus produced is separated into two sections using a distillation column as described in Example 1.
- the cutting point of the distillation is set at 100 ° C., the light fraction represents 50% by weight. starting gasoline.
- the light gasoline recovered at the outlet of the fractionation stage has diolefin, mercaptan and total sulfur content such that it can be used without additional treatment.
- Heavy gasoline requires a desulfurization step.
- step e The desulfurization of heavy petrol (steps e) and f) of the process according to the invention) is carried out using the device described in Example 2.
- the temperature of the catalytic zone comprising catalyst A is 290 ° C.
- the temperature of the catalytic zone containing the Catalyst B is 340 ° C.
- the gasoline thus produced has only a sulfur content of 26 ppm. It can be used without additional treatment. This gasoline is combined with the light gasoline recovered in step d) .
- This scheme carried out according to the invention makes it possible to produce a desulfurized gasoline with a limited loss of octane, the mercaptan and diolefin contents of which are compatible with the qualities required for gasolines.
- the desulfurization rate is 92.6%
- the residual sulfur content is 26 ppm
- the loss of octane calculated by the formula (RON + MON) / 2 is 2.15 points.
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Description
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Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0103358A FR2821850B1 (fr) | 2001-03-12 | 2001-03-12 | Procede de production d'essence a faible teneur en soufre comprenant une hydrogenation, un fractionnement, une etape de transformation des composes soufres et une desulfuration |
FR0103358 | 2001-03-12 | ||
FR0105538A FR2821852B1 (fr) | 2001-03-12 | 2001-04-23 | Procede de production d'une essence desulfuree a partir d'une coupe essence contenant de l'essence de conversion |
FR0105538 | 2001-04-23 | ||
PCT/FR2002/000351 WO2002072740A1 (fr) | 2001-03-12 | 2002-01-29 | Procede de production d'une essence desulfuree a partir d'une coupe essence contenant de l'essence de craquage |
Publications (2)
Publication Number | Publication Date |
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EP1370630A1 true EP1370630A1 (fr) | 2003-12-17 |
EP1370630B1 EP1370630B1 (fr) | 2004-10-13 |
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Application Number | Title | Priority Date | Filing Date |
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EP02701343A Expired - Lifetime EP1370630B1 (fr) | 2001-03-12 | 2002-01-29 | Procede de production d'une essence desulfuree a partir d'une coupe essence contenant de l'essence de craquage |
Country Status (11)
Country | Link |
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EP (1) | EP1370630B1 (fr) |
JP (1) | JP4385178B2 (fr) |
KR (1) | KR100813776B1 (fr) |
AT (1) | ATE279496T1 (fr) |
BR (1) | BR0208050B1 (fr) |
CA (1) | CA2440189C (fr) |
DE (1) | DE60201586T2 (fr) |
ES (1) | ES2231666T3 (fr) |
FR (1) | FR2821852B1 (fr) |
MX (1) | MXPA03008222A (fr) |
WO (1) | WO2002072740A1 (fr) |
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FR2884521B1 (fr) * | 2005-04-19 | 2009-08-21 | Inst Francais Du Petrole | Nouveau procede de desulfuration des essences par alourdissement des composes soufres |
FR2885137B1 (fr) * | 2005-04-28 | 2007-07-13 | Inst Francais Du Petrole | Procede de desulfuration d'essences olefiniques |
BR112019010168A2 (pt) * | 2016-11-23 | 2019-09-17 | Haldor Topsøe A/S | processo para dessulfurização de hidrocarbonetos |
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FR2797639B1 (fr) * | 1999-08-19 | 2001-09-21 | Inst Francais Du Petrole | Procede de production d'essences a faible teneur en soufre |
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2001
- 2001-04-23 FR FR0105538A patent/FR2821852B1/fr not_active Expired - Fee Related
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2002
- 2002-01-29 WO PCT/FR2002/000351 patent/WO2002072740A1/fr active IP Right Grant
- 2002-01-29 DE DE60201586T patent/DE60201586T2/de not_active Expired - Lifetime
- 2002-01-29 KR KR1020037011894A patent/KR100813776B1/ko not_active IP Right Cessation
- 2002-01-29 CA CA002440189A patent/CA2440189C/fr not_active Expired - Lifetime
- 2002-01-29 EP EP02701343A patent/EP1370630B1/fr not_active Expired - Lifetime
- 2002-01-29 JP JP2002571796A patent/JP4385178B2/ja not_active Expired - Fee Related
- 2002-01-29 AT AT02701343T patent/ATE279496T1/de not_active IP Right Cessation
- 2002-01-29 MX MXPA03008222A patent/MXPA03008222A/es active IP Right Grant
- 2002-01-29 BR BRPI0208050-8A patent/BR0208050B1/pt not_active IP Right Cessation
- 2002-01-29 ES ES02701343T patent/ES2231666T3/es not_active Expired - Lifetime
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Also Published As
Publication number | Publication date |
---|---|
FR2821852B1 (fr) | 2003-05-02 |
MXPA03008222A (es) | 2004-01-29 |
CA2440189C (fr) | 2009-12-15 |
EP1370630B1 (fr) | 2004-10-13 |
DE60201586T2 (de) | 2005-02-17 |
ES2231666T3 (es) | 2005-05-16 |
JP4385178B2 (ja) | 2009-12-16 |
BR0208050B1 (pt) | 2014-11-25 |
JP2004523629A (ja) | 2004-08-05 |
ATE279496T1 (de) | 2004-10-15 |
KR20030080084A (ko) | 2003-10-10 |
DE60201586D1 (de) | 2004-11-18 |
WO2002072740A1 (fr) | 2002-09-19 |
FR2821852A1 (fr) | 2002-09-13 |
KR100813776B1 (ko) | 2008-03-13 |
CA2440189A1 (fr) | 2002-09-19 |
BR0208050A (pt) | 2004-02-25 |
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