EP1445299B1 - Verfahren zur Gewinnung einer Beschickung zu einem Veretherungsverfahren - Google Patents
Verfahren zur Gewinnung einer Beschickung zu einem Veretherungsverfahren Download PDFInfo
- Publication number
- EP1445299B1 EP1445299B1 EP04290069A EP04290069A EP1445299B1 EP 1445299 B1 EP1445299 B1 EP 1445299B1 EP 04290069 A EP04290069 A EP 04290069A EP 04290069 A EP04290069 A EP 04290069A EP 1445299 B1 EP1445299 B1 EP 1445299B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- process according
- nitrogen
- compounds
- metal
- containing compounds
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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- 238000000034 method Methods 0.000 title claims description 28
- 238000006266 etherification reaction Methods 0.000 title claims description 14
- 150000001993 dienes Chemical class 0.000 claims description 25
- 229930195733 hydrocarbon Natural products 0.000 claims description 23
- 150000002430 hydrocarbons Chemical class 0.000 claims description 23
- 239000004215 Carbon black (E152) Substances 0.000 claims description 16
- 239000003054 catalyst Substances 0.000 claims description 15
- 238000005984 hydrogenation reaction Methods 0.000 claims description 14
- 150000002825 nitriles Chemical class 0.000 claims description 12
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 11
- 150000001336 alkenes Chemical class 0.000 claims description 10
- 150000001875 compounds Chemical class 0.000 claims description 10
- 229910052751 metal Inorganic materials 0.000 claims description 10
- 239000002184 metal Substances 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 8
- 239000011593 sulfur Substances 0.000 claims description 7
- 229910052717 sulfur Inorganic materials 0.000 claims description 7
- 238000009835 boiling Methods 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- -1 diene compounds Chemical class 0.000 claims description 5
- 238000005194 fractionation Methods 0.000 claims description 5
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 5
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 4
- 230000000737 periodic effect Effects 0.000 claims description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical group [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 3
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011733 molybdenum Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 2
- 229910052721 tungsten Inorganic materials 0.000 claims description 2
- 239000010937 tungsten Substances 0.000 claims description 2
- 239000000758 substrate Substances 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 42
- 229910017464 nitrogen compound Inorganic materials 0.000 description 20
- 229910052757 nitrogen Inorganic materials 0.000 description 19
- 150000002830 nitrogen compounds Chemical class 0.000 description 19
- 150000003464 sulfur compounds Chemical class 0.000 description 15
- 238000005259 measurement Methods 0.000 description 7
- 125000004432 carbon atom Chemical group C* 0.000 description 6
- 238000005406 washing Methods 0.000 description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 4
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000001577 simple distillation Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000003377 acid catalyst Substances 0.000 description 2
- 150000008064 anhydrides Chemical class 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- 229930192474 thiophene Natural products 0.000 description 2
- VDMXPMYSWFDBJB-UHFFFAOYSA-N 1-ethoxypentane Chemical group CCCCCOCC VDMXPMYSWFDBJB-UHFFFAOYSA-N 0.000 description 1
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241000861223 Issus Species 0.000 description 1
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical class COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 1
- OFOBLEOULBTSOW-UHFFFAOYSA-N Propanedioic acid Natural products OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 150000007514 bases Chemical class 0.000 description 1
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- VZCYOOQTPOCHFL-UPHRSURJSA-N maleic acid Chemical compound OC(=O)\C=C/C(O)=O VZCYOOQTPOCHFL-UPHRSURJSA-N 0.000 description 1
- 239000011976 maleic acid Substances 0.000 description 1
- 150000002826 nitrites Chemical class 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000002798 polar solvent Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- FVSKHRXBFJPNKK-UHFFFAOYSA-N propionitrile Chemical compound CCC#N FVSKHRXBFJPNKK-UHFFFAOYSA-N 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- HVZJRWJGKQPSFL-UHFFFAOYSA-N tert-Amyl methyl ether Chemical compound CCC(C)(C)OC HVZJRWJGKQPSFL-UHFFFAOYSA-N 0.000 description 1
- NUMQCACRALPSHD-UHFFFAOYSA-N tert-butyl ethyl ether Chemical class CCOC(C)(C)C NUMQCACRALPSHD-UHFFFAOYSA-N 0.000 description 1
- VZCYOOQTPOCHFL-UHFFFAOYSA-N trans-butenedioic acid Natural products OC(=O)C=CC(O)=O VZCYOOQTPOCHFL-UHFFFAOYSA-N 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/32—Selective hydrogenation of the diolefin or acetylene 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Definitions
- the present invention relates to a process for obtaining a hydrocarbon fraction that can be used as a feedstock of an etherification unit and that contains a reduced quantity of diene, nitrogen and sulfur compounds, from an initial charge of hydrocarbons.
- the present invention finds application in the treatment of gasolines with a view to obtaining a fraction comprising olefins containing from 4 to 6 carbon atoms, and having a reduced content of diene, nitrile, nitrogen and sulfur compounds.
- this fraction can then be used to supply etherification units, for example in order to produce methyl tertiary butyl ethers (MTBE), ethyl tertiary butyl ethers (ETBE), tertiary amyl methyl ether (TAME) or tertiary amyl ethyl ether ( TAEE)
- the request for WO 96/00714 proposes a method for reducing the content of pollutants present in the charges for etherification units, by selective hydrogenation.
- the pollutants eliminated by this process are nitriles and diolefins.
- the diolefins are initially hydrogenated to olefins, and then the nitriles are hydrogenated to amines.
- the catalyst used in this step is a catalyst comprising cobalt. Since amines are basic compounds, they are then easily extracted by washing with water. This method therefore also requires the implementation of a washing step to remove the nitrogen compounds in the form of amines and thus has the aforementioned drawback of the reprocessing of the washing solutions.
- the US Patent 6,469,223 describes a process for the selective hydrogenation of dienes in a hydrocarbon feedstock.
- the present invention provides a cost-effective and simple way of eliminating, at least partially, the dienes, the nitrile-type nitrogen compounds and the light sulfur compounds present in the initial gasoline.
- the method used according to the invention comprises at least two stages: a first stage of selective hydrogenation of the whole of the initial hydrocarbon feedstock and a second stage of fractionation of said hydrogenated feedstock.
- This step is intended to at least partially remove the diolefins present in the initial hydrocarbon feed, such as preferably a gasoline cut.
- Diolefins are precursors of gums which polymerize in the etherification reactors and limit their life as well as nitrile-type nitrogen compounds (whose formula is given below). It has indeed been found by the applicant that under the experimental conditions mentioned in the rest of the description, said nitriles are converted into heavy nitrogen compounds which respond positively to the measurement of basic nitrogen.
- Nitrite compounds R - C ⁇ N, where R comprises from 1 to 6 carbon atoms.
- This step also makes it possible to convert light sulfur compounds such as mercaptans, sulphides and CS2, whose boiling point is generally lower than that of thiophene, into heavier sulfur compounds whose boiling point is higher than that of thiophene.
- Said selective hydrogenation step generally takes place in the presence of a catalyst comprising at least one metal of group VIII of the periodic table, preferably chosen from the group formed by platinum, palladium and nickel, and a support.
- the cobalt may also be chosen from said group.
- a catalyst containing 1 to 20% by weight of nickel deposited on an inert support such as, for example, alumina, silica, silica-alumina, a nickel aluminate or a support containing at least 50% alumina.
- Another Group VIB metal of the Periodic Table can be combined with this group VIII metal to form a bimetallic catalyst, such as, for example, molybdenum or tungsten. This group VIB metal is preferably deposited at a level of 1% by weight at 20% by weight on the support.
- the choice of operating conditions is particularly important according to the invention.
- the operation will generally be carried out under pressure in the presence of a quantity of hydrogen in small excess relative to the stoichiometric value necessary for hydrogenating the diolefins.
- hydrogen and the feedstock to be treated are injected in ascending or descending streams into a preferably fixed catalyst bed reactor.
- the temperature is most generally between 50 and 300 ° C, and preferably between 80 and 250 ° C, and very preferably between 120 and 210 ° C.
- the pressure is chosen to be sufficient to maintain more than 80%, and preferably more than 95% by weight of the gasoline to be treated in liquid form in the reactor; it is most generally between 0.4 and 5 MPa inclusive, and preferably greater than 1 MPa.
- An advantageous pressure is between 1 to 4 MPa inclusive.
- the space velocity is, in these conditions of the order of 1 to 12 h -1 , preferably of the order of 2 to 10 h -1 .
- the initial hydrocarbon feedstock such as a petrol cut may contain up to a few% by weight of diolefins. After hydrogenation, the diolefin content is most often reduced to less than 5000 ppm, preferably less than 2500 ppm, or even less than 1500 ppm.
- step a) takes place in a catalytic hydrogenation reactor which comprises a catalytic reaction zone traversed by the entire charge and the amount of hydrogen necessary to effect the desired reactions.
- the nitrogen compounds derived from step a) are compounds with a boiling point greater than those of hydrocarbons comprising 5 carbon atoms.
- these compounds react with the measurement of basic nitrogen according to the ASTM4739 method.
- Step b) consists of a separation of the nitrogen compounds by distillation.
- the effluents resulting from stage a) are fractionated in order to produce at least two sections, a light fraction comprising the majority of the hydrocarbons, and mainly olefins containing 4 or 5 carbon atoms and free of nitrogen compounds, and a heavy fraction concentrating heavy hydrocarbons and nitrogen compounds weighed up during step a).
- this preferred embodiment also makes it possible to at least partially eliminate the sulfur compounds of said light fraction.
- the nitrogen compound content of the light fraction of the gasoline from step b) generally contains less than 20 ppm nitrogen, preferably less than 10 ppm nitrogen, and very preferably less than 5 ppm nitrogen.
- the content of light sulfur compounds in the light fraction of gasoline is generally less than 200 ppm, preferably less than 100 ppm, and very preferably less than 50 ppm sulfur.
- Table 1 summarizes the characteristics of gasoline A as well as the 3 fractions obtained by distillation. ⁇ u> Table 1 ⁇ / u> Essence A PI-55 55-140 140+ Density 0.716 .6504 .7382 0.842 Basic nitrogen (ppm) 9 1 1 71 Total nitrogen (ppm) 21 15 13 110 MAV (mg / g) 14 6.5 15.5 30 HBr 101 130 79 48 S (ppm) 780 92 926 2563 Yield (% wt) 100 29.59 64.27 6.14
- the light gasoline corresponding to the PI-55 cut concentrates the majority of the light olefins (C4 and C5). It therefore constitutes the etherification charge. This fraction comprises 15 ppm of nitrogen, 92 ppm of sulfur and a MAV (maleic acid value) of 6.5, which corresponds to almost 0.8% by weight of diolefins. This gasoline treated on an acidic etherification catalyst would cause a premature deactivation thereof.
- Example below is in accordance with the present invention.
- the initial charge used is similar to that of Example 1.
- gasoline produced (gasoline B) is distilled in three sections (step b)).
- Step a) is carried out as follows: gasoline A is treated on a fixed bed reactor charged with HR845® catalyst based on nickel and molybdenum marketed by Axens, in the presence of hydrogen. The reaction is carried out at 165 ° C. under a pressure of 20 bar (2 MPa) and a space velocity of 4 h -1 . The H 2 / charge ratio expressed in liter of hydrogen per liter of feedstock is 6. The gasoline thus produced during step a) is gasoline B, the characteristics of which are given in Table 2.
- Gasoline B is then fractionated by distillation into 3 fractions whose cutting points are identical to the fractions of Example 1.
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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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Claims (8)
- Verfahren zur Gewinnung einer Kohlenwasserstofffraktion, die als Charge einer Veretherungsanlage verwendet werden kann und eine verringerte Menge an dienischen, stickstoffhaltigen und schwefelhaltigen Verbindungen enthält, ausgehend von einer Ursprungscharge an Kohlenwasserstoffen, die eine Mischung aus Olefinen, Dienen, Nitrilen sowie schwefelhaltigen Verbindungen umfasst, wobei das Verfahren mindestens die folgenden, nacheinander durchgeführten Schritte umfasst:a) eine selektive Hydrierung der Ursprungscharge an Kohlenwasserstoffen, in Gegenwart eines Katalysators, der mindestens ein Metall der Gruppe VIII und ein weiteres Metall der Gruppe VIB des Periodensystems umfasst,b) eine Fraktionierung durch Destillation der Stoffströme, die in Schritt a) entstehen, unter Bedingungen, die es ermöglichen, mindestens zwei Fraktionen zu erhalten, darunter- die Kohlenwasserstofffraktion, welche einen Siedepunkt von weniger als 60 °C aufweist und eine verringerte Menge an dienischen, stickstoffhaltigen und schwefelhaltigen Verbindungen umfasst, und- eine Schwerfraktion, welche die schwerflüchtigen Kohlenwasserstoffe und den überwiegenden Anteil der stickstoffhaltigen und schwefelhaltigen Verbindungen, die in Schritt a) entstehen, enthält.
- Verfahren nach Anspruch 1, wobei das Metall der Gruppe VIII aus der Gruppe ausgewählt ist, die aus Platin, Palladium, Nickel besteht.
- Verfahren nach Anspruch 2, wobei der Katalysator 1 Gew.-% bis 20 Gew.-% an Nickel enthält, welches auf einen inerten Träger aufgebracht ist.
- Verfahren nach Anspruch 1, wobei es sich bei dem Metall der Gruppe VIII um Kobalt handelt.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei der Katalysator 1 Gew.-% bis 20 Gew.-% an Metall der Gruppe VIB umfasst.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei es sich bei dem Metall der VIB um Molybdän oder Wolfram handelt.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei der Katalysator unter einem Druck von 0,4 bis 5 MPa, bei einer Temperatur von 50 bis 300 °C eingesetzt wird, mit einer stundenbezogenen Raumgeschwindigkeit der Charge von 1 h-1 bis 12 h-1.
- Verfahren nach einem der vorhergehenden Ansprüche, wobei die Hydrierung in Gegenwart einer Wasserstoffmenge durchgeführt wird, die einen geringfügigen Überschuss darstellt, unter Bezugnahme auf den stöchiometrischen Wert, welcher erforderlich ist, um die Gesamtheit der Diene, die in der Ursprungscharge an Kohlenwasserstoffen enthalten sind, zu hydrieren.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0300693A FR2850113B1 (fr) | 2003-01-22 | 2003-01-22 | Procede d'obtention d'une charge utilisable dans une unite d'etherification |
FR0300693 | 2003-01-22 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1445299A1 EP1445299A1 (de) | 2004-08-11 |
EP1445299B1 true EP1445299B1 (de) | 2012-03-14 |
Family
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Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP04290069A Expired - Lifetime EP1445299B1 (de) | 2003-01-22 | 2004-01-09 | Verfahren zur Gewinnung einer Beschickung zu einem Veretherungsverfahren |
Country Status (4)
Country | Link |
---|---|
US (1) | US7025872B2 (de) |
EP (1) | EP1445299B1 (de) |
ES (1) | ES2381785T3 (de) |
FR (1) | FR2850113B1 (de) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN100389874C (zh) * | 2006-07-14 | 2008-05-28 | 谷育英 | 一种用于c5石油树脂中烯烃加氢反应催化剂及其制备方法和应用 |
US7553995B2 (en) * | 2007-09-11 | 2009-06-30 | Catalytic Distillation Technologies | Method of producing tertiary amyl ethyl ether |
EP2816094B1 (de) | 2013-06-19 | 2020-04-29 | IFP Energies nouvelles | Herstellungsverfahren einer essenz mit niedrigem schwefel- und mercaptangehalt |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4175033A (en) * | 1976-05-06 | 1979-11-20 | Uop Inc. | Hydroprocessing of hydrocarbons over nickel, moly, platinum catalyst |
US5321163A (en) * | 1993-09-09 | 1994-06-14 | Chemical Research & Licensing Company | Multi-purpose catalytic distillation column and eterification process using same |
WO1996017903A1 (en) * | 1994-11-25 | 1996-06-13 | Kvaerner Process Technology Ltd | Multi-step hydrodesulfurization process |
US5712415A (en) * | 1994-12-13 | 1998-01-27 | Intevep, S.A. | Process for the simultaneous selective hydrogenation of diolefins and nitriles |
US5948942A (en) * | 1994-12-13 | 1999-09-07 | Intevep, S.A. | Bimetallic catalyst for the simultaneous selective hydrogenation of diolefins and nitriles and method of making same |
US6210561B1 (en) * | 1996-08-15 | 2001-04-03 | Exxon Chemical Patents Inc. | Steam cracking of hydrotreated and hydrogenated hydrocarbon feeds |
US6042719A (en) * | 1998-11-16 | 2000-03-28 | Mobil Oil Corporation | Deep desulfurization of FCC gasoline at low temperatures to maximize octane-barrel value |
US6123830A (en) * | 1998-12-30 | 2000-09-26 | Exxon Research And Engineering Co. | Integrated staged catalytic cracking and staged hydroprocessing process |
US6469223B2 (en) * | 2000-01-04 | 2002-10-22 | Fina Technology, Inc. | Selective hydrogenation of dienes |
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 |
US20040178123A1 (en) * | 2003-03-13 | 2004-09-16 | Catalytic Distillation Technologies | Process for the hydrodesulfurization of naphtha |
-
2003
- 2003-01-22 FR FR0300693A patent/FR2850113B1/fr not_active Expired - Lifetime
-
2004
- 2004-01-09 EP EP04290069A patent/EP1445299B1/de not_active Expired - Lifetime
- 2004-01-09 ES ES04290069T patent/ES2381785T3/es not_active Expired - Lifetime
- 2004-01-22 US US10/761,240 patent/US7025872B2/en not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
EP1445299A1 (de) | 2004-08-11 |
ES2381785T3 (es) | 2012-05-31 |
FR2850113A1 (fr) | 2004-07-23 |
US20040167363A1 (en) | 2004-08-26 |
FR2850113B1 (fr) | 2007-03-02 |
US7025872B2 (en) | 2006-04-11 |
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