EP1659163A1 - Verfahren zur Umwandlung von gesättigten Schwefelverbindungen eines Kohlenwasserstoffschnitty mit wenig oder keinen Olefinen - Google Patents

Verfahren zur Umwandlung von gesättigten Schwefelverbindungen eines Kohlenwasserstoffschnitty mit wenig oder keinen Olefinen Download PDF

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Publication number
EP1659163A1
EP1659163A1 EP05292373A EP05292373A EP1659163A1 EP 1659163 A1 EP1659163 A1 EP 1659163A1 EP 05292373 A EP05292373 A EP 05292373A EP 05292373 A EP05292373 A EP 05292373A EP 1659163 A1 EP1659163 A1 EP 1659163A1
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EP
European Patent Office
Prior art keywords
mercaptans
olefins
sulfur compounds
converting
reaction step
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EP05292373A
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English (en)
French (fr)
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EP1659163B1 (de
Inventor
Sébastien Leplat
Florent Picard
Nathalie Marchal
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil

Definitions

  • the invention relates to a process for softening and desulfurizing hydrocarbon fractions generally containing less than 1% by weight of olefins, and sulfur mainly in the form of mercaptans.
  • the process described in the present invention is particularly suitable for the treatment of hydrocarbon fractions derived from atmospheric distillation, such as, for example, gasoline, kerosene or light gas oil fractions. These hydrocarbon fractions contain varying amounts of mercaptans which give them a corrosive and malodorous acid character.
  • the solutions generally used to treat these mercaptans consist of oxidizing the mercaptans to disulfides, and then separating the latter, which are heavier, generally by distillation.
  • the present invention provides a technical solution for softening the fractions to be treated by converting the mercaptans to sulphides, and optionally to desulfurize the fractions to be treated by separating the sulphides thus formed.
  • the process consists in mixing the hydrocarbon fraction to be treated with, on the one hand, another hydrocarbon fraction containing unsaturated compounds, and on the other hand with hydrogen, then on passing the mixture over a metal sulphide catalyst in optimized conditions to promote the addition of mercaptans to the unsaturated compounds to form sulphide sulfur compounds.
  • the sulfur compounds thus transformed have a boiling point higher than their initial temperature and can then be separated to recover a sulfur-depleted hydrocarbon fraction.
  • the reduction of the mercaptan content in the hydrocarbon fractions directly from atmospheric distillation is generally carried out by a so-called "softening" process.
  • Many softening processes do not implement the reduction of the overall sulfur content, but only the dimerization of the mercaptans to disulfides to meet specifications.
  • This oxidation of mercaptans is generally carried out catalytically using oxygen as the oxidizing agent.
  • the extractive softening processes make it possible to subtract the sulfur from the feedstock. They consist in contacting the distillate to be treated with a basic aqueous solution (most often based on sodium hydroxide) which makes it possible to recover the mercaptans.
  • the softening of the hydrocarbon fractions may also be carried out by addition reaction of the mercaptans to the diolefins.
  • These reactions are in particular envisaged in the case of the treatment of gasolines containing both mercaptans and unsaturated hydrocarbon compounds, such as, for example, FCC (Fluid Catalytic Cracking) gasolines in which the unsaturated compounds, which are most often olefinic in nature, are widely present.
  • FCC Fluid Catalytic Cracking
  • Patent FR 2821851 A1 also describes a process for weighing mercaptans by addition to olefins using a catalyst comprising at least one Group VIII element.
  • a catalyst comprising at least one Group VIII element.
  • the same type of reactions is contemplated in US Patent 5,659,106A on an acid catalyst such as a sulfonated resin. In this case, the reaction is carried out in the absence of hydrogen.
  • Non-catalytic solutions are also presented in the literature.
  • a softening method involving unsaturated compounds is developed.
  • a saturated mercaptan-rich naphtha is treated by adding an olefinic compound (from 1 to 10% by weight) in the presence of a phenylene diamine inhibitor, at a rate of 0.0001% to 1% weight. After a sufficient storage period, the mercaptan concentration of the mixture meets the specifications.
  • the process described in the present invention provides a solution for partially softening or partially desulfurizing hydrocarbon fractions that are free of olefins or contain low levels of unsaturated compounds.
  • the process described in the present invention is particularly suitable for the treatment of hydrocarbon fractions derived from atmospheric distillation, such as, for example, gasoline, kerosene or light gas oil fractions.
  • the process consists in mixing, with the hydrocarbon fraction to be treated, hydrogen and possibly another hydrocarbon fraction containing olefinic olefins.
  • This olefinic fraction is generally derived from cracking processes such as the FCC, the steam cracker, or a coking unit.
  • Hydrogen can come from any source in the refinery. The quantities of hydrogen required are generally low enough not to require the complementary implantation of a dedicated hydrogen production unit.
  • the resulting mixture must be such that on the one hand the molar ratio H 2 / olefins is between 0.03 and 2, preferably between 0.05 and 1, so more preferably between 0.2 and 0.8, and secondly the molar ratio olefins / mercaptans is between 5 and 5000 and preferably between 10 and 1000, more preferably between 80 and 600, or even between 150 and 400 .
  • the mixture corresponding to the two preceding conditions is then injected into a reactor containing a catalyst capable of reacting the saturated sulfur compounds such as the mercaptans present. To be effective, the reaction must be carried out in the presence of hydrogen.
  • the non-olefinic feedstock treated is a gasoline fraction resulting from atmospheric distillation, the boiling point of which is less than 250.degree. C., and preferably less than 220.degree.
  • the charge to be treated may itself contain a certain amount of olefins to which it will be necessary to add only a quantity of hydrogen determined to be in the range of ratio H2 olefins defined above, namely between 0.03 and 2, and preferably between 0.05 and 1.
  • the latter will generally come from an olefinic gasoline such as for example a cracking gasoline generally from a catalytic or thermal cracking unit.
  • the process for converting the mercaptans contained in a hydrocarbon feedstock containing less than 1% olefins according to the invention may comprise an additional step of separating the sulfur compounds formed during the reaction step, so as to produce an effluent containing less than 50% by weight of the sulfur compounds present in the feed, and a cut containing the majority of the sulfur compounds.
  • the process according to the invention thus makes it possible to convert the mercaptans into heavier sulfur compounds with a conversion rate generally of at least 50% by weight.
  • the olefinic fractions present in the refinery are generally derived from cracking units such as catalytic cracking, thermal cracking or steam cracking.
  • the boiling temperatures of this olefinic fraction are generally below 250 ° C. However, it is preferable to use hydrocarbon fractions containing olefins with 4, 5 or 6 carbon atoms in order to improve the yield of the weighting reaction of the sulfur compounds. Hydrogen is also most often from the refinery. Hydrogen substantially free of H 2 S is used because this compound can react with olefins to form undesirable sulfur compounds.
  • the hydrogen may come either from a specific hydrogen production unit or, for example, from the catalytic reforming unit of the gasolines.
  • the reaction step consists of passing the mixture formed at the end of the mixing step on a catalyst operated in a fixed bed, under optimized operating conditions.
  • the catalyst used in the reactor is a catalyst comprising at least one Group VIII metal deposited on an inert support based on porous metal oxide.
  • the support is made of alumina, silica, titanium oxide or contains at least 50% alumina.
  • Another Group VIb metal may be associated with the Group VIII metal to form a bimetallic catalyst.
  • the amount of Group VIII metal in oxide form is between 1% and 30% by weight.
  • the amount of metal of group Vlb in oxide form is between 0% and 20% by weight.
  • Nickel-based catalysts or catalysts based on mixed nickel and molybdenum or tungsten oxide are preferably used.
  • the catalyst used in the reaction stage contains between 1 and 30% by weight of NiO and between 0% and 20% by weight of MoO 3 .
  • the catalyst may undergo a preliminary sulphurization step in order to convert the metal oxides to sulphides. Sulfurization is carried out in the presence of H 2 S, either directly injected in a mixture with hydrogen, or generated in situ in the reactor by hydrogenolysis of a sulfur compound, so that the metal sulphidation rate of the catalyst is greater than 50%, and preferably greater than 90%.
  • the temperature of the reactor is generally between 100 ° C. and 250 ° C., and preferably between 140 ° C. and 200 ° C.
  • the reactor is operated at a pressure of between 0.5 MPa and 5 MPa, and preferably between 1 MPa and 3 MPa, and at a VVH between 1 h -1 and 10 h -1, and preferably between 1, 5 h -1 and 8 h -1 .
  • the flow of hydrogen is generally adjusted to obtain a molar ratio between hydrogen and olefins of between 0.03 and 2 and preferably between 0.05 and 1.
  • the saturated sulfur compounds present in the feed are converted into saturated sulfur compounds of higher boiling point.
  • the saturated compounds belong to the families consisting of mercaptans, sulphides and CS 2 .
  • the conversion is measured by the conversion rate of mercaptans into heavier compounds, ie having a higher boiling point.
  • the molar ratio between the olefins and hydrogen is optimized in order to limit the deactivation of the catalyst by the carbon deposition from the olefinic compounds. In the absence of hydrogen, the catalyst undergoes a strong deactivation, and the conversion rate of the mercaptans is significantly reduced.
  • the effluent is depleted in light saturated sulfur compounds and more particularly in mercaptans.
  • the degree of conversion of the mercaptans containing 1 to 4 carbon atoms is generally between 50% and 100%.
  • the fraction thus produced is therefore softened in the sense well known to those skilled in the art.
  • a third step can be carried out optionally if one seeks to reduce the sulfur content of the feedstock to be treated.
  • This third step consists in separating the sulfur compounds formed during the reaction stage from the hydrocarbon effluent of said reaction stage.
  • the separation step may consist of any method capable of achieving this separation. However, it will be preferred to use a physical separation method based on the boiling temperatures of the compounds to be separated, such as, for example, a simple flash, or distillation in a distillation column.
  • the light fraction recovered at the top of the column contains the majority of the saturated hydrocarbon fraction, and is depleted in sulfur compounds and in mercaptans.
  • the heavy fraction recovered at the bottom of the column concentrates the sulfur compounds formed during the reaction step. This fraction can be treated in a hydrodesulfurization unit to extract the sulfur.
  • the implementation of the separation step subsequent to the reaction step therefore allows to desulfurize the hydrocarbon feedstock to be treated without resorting to a conventional hydrodesulphurization process for at least a portion of the hydrocarbon effluent.
  • a series of tests was conducted in a pilot unit loaded with 100 cm 3 of catalyst.
  • the catalyst used contains nickel and molybdenum on an alumina support (catalyst marketed under the reference HR845 by the company Axens). Before the charge is injected, the catalyst is sulphurated with an H 2 + H 2 S mixture at 350 ° C. During the tests, the temperature, the pressure and the space velocity are kept constant at 180 ° C., 2.5 MPa and 4 h -1 respectively for all the tests carried out.
  • a gasoline A of atmospheric distillation of a crude oil is injected into a reactor in the absence of hydrogen.
  • the effluent B1 is separated by distillation into two fractions with a cutting point corresponding to a temperature of 100 ° C.
  • the two fractions obtained are denoted LCN1 (light fraction) and HCN1 (heavy fraction).
  • LCN1 light fraction
  • HCN1 heavy fraction
  • the presence of the catalyst makes it possible to reduce the mercaptan content by 20%.
  • the mercaptan content of the LCN1 cut remains high, and the distribution of the mercaptans between the LCN1 cuts and the HCN1 shows that the observed conversion equally affects the light mercaptans and the heavy mercaptans, of at least five carbon atoms. .
  • the organic sulfur content remains unchanged during the treatment on the catalyst.
  • the sulfur of this fraction is found exclusively in the form of mercaptans, which has the consequence of concentrating the non-mercaptan sulfur in the heavy fraction.
  • Gasoline A is mixed with an olefinic cracking gasoline C obtained from a catalytic cracking unit before being injected into the reactor in the presence of hydrogen at the rate of 5 liters of hydrogen per liter of feedstock.
  • Gasoline C represents 10% by weight of the mixture noted as D1 gasoline .
  • the gasoline D1 mixed with hydrogen is injected onto the catalyst.
  • the effluent B2 is separated by distillation into two fractions with a cutting point corresponding to a temperature of 100 ° C.
  • the two fractions obtained are denoted LCN2 (light fraction) and HCN2 (heavy fraction).
  • Table 2 presents the characteristics of species A, C and D1. The characteristics of the different sections are summarized in Table 3.
  • the simultaneous presence of olefins and hydrogen in the mixture D1 makes it possible to reduce the initial mercaptan content by 57%.
  • the conversion is three times greater than that observed in Example 1.
  • the distribution of mercaptans between LCN2 sections and HCN2 is largely modified, the light mercaptans contained in the LCN2 section are preferentially converted.
  • Gasoline A is mixed with gasoline C before being injected into the reactor in the presence of hydrogen at 5 liters of hydrogen per liter of feed.
  • Gasoline C represents 20% by weight of the mixture noted as D2 gasoline .
  • the effluent B3 is separated by distillation into two fractions with a cutting point corresponding to a temperature of 100 ° C.
  • the two fractions obtained are denoted LCN3 (light fraction) and HCN3 (heavy fraction).
  • Table 4 presents the characteristics of species A, C and D2. Those of the different sections are grouped together in Table 5.
  • Gasoline A is mixed with gasoline C before being injected into the reactor in the presence of hydrogen at a rate of 10 liters of hydrogen per liter of feedstock.
  • Gasoline C representing 10% of the mixture which is noted the essence D3.
  • the effluent B4 is separated by distillation into two fractions with a cutting point corresponding to a temperature of 100 ° C.
  • the two fractions obtained are denoted LCN4 (light fraction) and HCN4 (heavy fraction).
  • Table 6 groups the characteristics of the different species.
  • H 2 / olefins ratio must also be optimized to limit the deactivation of the catalyst, the hydrogen consumption and the saturation of the olefins.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP05292373A 2004-11-17 2005-11-08 Verfahren zur Umwandlung von gesättigten Schwefelverbindungen eines Kohlenwasserstoffschnitty mit wenig oder keinen Olefinen Active EP1659163B1 (de)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR0412206A FR2877951B1 (fr) 2004-11-17 2004-11-17 Procede de transformation des composes soufres satures d'une coupe hydrocarbonee contenant peu ou pas d'olefines

Publications (2)

Publication Number Publication Date
EP1659163A1 true EP1659163A1 (de) 2006-05-24
EP1659163B1 EP1659163B1 (de) 2009-03-11

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EP05292373A Active EP1659163B1 (de) 2004-11-17 2005-11-08 Verfahren zur Umwandlung von gesättigten Schwefelverbindungen eines Kohlenwasserstoffschnitty mit wenig oder keinen Olefinen

Country Status (4)

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US (1) US20060124508A1 (de)
EP (1) EP1659163B1 (de)
DE (1) DE602005013173D1 (de)
FR (1) FR2877951B1 (de)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8461293B2 (en) 2010-08-03 2013-06-11 Chevron Phillips Chemical Company Lp Methods of mercaptanizing olefinic hydrocarbons and compositions produced therefrom

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2255394A (en) 1938-11-09 1941-09-09 Phillips Petroleum Co Process for treating oils
US2546345A (en) 1950-03-04 1951-03-27 Texas Co Dethiolizing hydrocarbons
US2694034A (en) 1950-06-30 1954-11-09 Universal Oil Prod Co Treatment of saturated distillates
GB763625A (en) 1953-02-06 1956-12-12 Gelsenberg Benzin Ag Improvements in or relating to the purification of hydrocarbons
US2808365A (en) 1955-02-07 1957-10-01 Sun Oil Co Petroleum refining
US2853431A (en) 1955-05-31 1958-09-23 Sun Oil Co Sweetening petroleum hydrocarbons with a nu, nu'-dialkyl-phenylene diamine and oxygen in the presence of refinery slop oil
US3053756A (en) 1958-07-03 1962-09-11 Basf Ag Refining of industrial hydrocarbon mixtures
US3574093A (en) 1969-01-22 1971-04-06 Universal Oil Prod Co Combination process for treatment of hydrocarbon streams containing mercapto compounds
US5659106A (en) 1995-06-22 1997-08-19 Uop Catalytic distillation process for mercaptan and olefin removal
FR2821851A1 (fr) 2001-03-12 2002-09-13 Inst Francais Du Petrole Procede de production d'essence a faible teneur en soufre comprenant une etape de transformation des composes soufres, un traitement sur catalyseur acide et une desulfuration
US20020166798A1 (en) * 2001-03-12 2002-11-14 Institute Francais Du Petrole Process for the production of gasoline with a low sulfur content comprising a stage for transformation of sulfur-containing compounds, an acid-catalyst treatment and a desulfurization
US20030094399A1 (en) 2001-09-28 2003-05-22 Catalytic Distillation Technologies Process for the desulfurization of FCC naphtha

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3894941A (en) * 1973-12-14 1975-07-15 Gulf Research Development Co Process for converting mercaptans to alkyl sulfides
FR2476118B1 (fr) * 1980-02-19 1987-03-20 Inst Francais Du Petrole Procede de desulfuration d'un effluent de craquage catalytique ou de craquage a la vapeur
FR2807061B1 (fr) * 2000-03-29 2002-05-31 Inst Francais Du Petrole Procede de desulfuration d'essence comprenant une desulfuration des fractions lourde et intermediaire issues d'un fractionnement en au moins trois coupes

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2255394A (en) 1938-11-09 1941-09-09 Phillips Petroleum Co Process for treating oils
US2546345A (en) 1950-03-04 1951-03-27 Texas Co Dethiolizing hydrocarbons
US2694034A (en) 1950-06-30 1954-11-09 Universal Oil Prod Co Treatment of saturated distillates
GB763625A (en) 1953-02-06 1956-12-12 Gelsenberg Benzin Ag Improvements in or relating to the purification of hydrocarbons
US2808365A (en) 1955-02-07 1957-10-01 Sun Oil Co Petroleum refining
US2853431A (en) 1955-05-31 1958-09-23 Sun Oil Co Sweetening petroleum hydrocarbons with a nu, nu'-dialkyl-phenylene diamine and oxygen in the presence of refinery slop oil
US3053756A (en) 1958-07-03 1962-09-11 Basf Ag Refining of industrial hydrocarbon mixtures
US3574093A (en) 1969-01-22 1971-04-06 Universal Oil Prod Co Combination process for treatment of hydrocarbon streams containing mercapto compounds
US5659106A (en) 1995-06-22 1997-08-19 Uop Catalytic distillation process for mercaptan and olefin removal
FR2821851A1 (fr) 2001-03-12 2002-09-13 Inst Francais Du Petrole Procede de production d'essence a faible teneur en soufre comprenant une etape de transformation des composes soufres, un traitement sur catalyseur acide et une desulfuration
US20020166798A1 (en) * 2001-03-12 2002-11-14 Institute Francais Du Petrole Process for the production of gasoline with a low sulfur content comprising a stage for transformation of sulfur-containing compounds, an acid-catalyst treatment and a desulfurization
US20030094399A1 (en) 2001-09-28 2003-05-22 Catalytic Distillation Technologies Process for the desulfurization of FCC naphtha

Also Published As

Publication number Publication date
FR2877951A1 (fr) 2006-05-19
FR2877951B1 (fr) 2006-12-22
EP1659163B1 (de) 2009-03-11
US20060124508A1 (en) 2006-06-15
DE602005013173D1 (de) 2009-04-23

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