EP0773981A1 - Jet fuel and method for producing same - Google Patents
Jet fuel and method for producing sameInfo
- Publication number
- EP0773981A1 EP0773981A1 EP96917528A EP96917528A EP0773981A1 EP 0773981 A1 EP0773981 A1 EP 0773981A1 EP 96917528 A EP96917528 A EP 96917528A EP 96917528 A EP96917528 A EP 96917528A EP 0773981 A1 EP0773981 A1 EP 0773981A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- jet fuel
- ratio
- jet
- decaline
- catalyst
- 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
- 239000000446 fuel Substances 0.000 title claims abstract description 79
- 238000004519 manufacturing process Methods 0.000 title description 9
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 19
- 238000000034 method Methods 0.000 claims abstract description 19
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 13
- 239000011593 sulfur Substances 0.000 claims abstract description 13
- NNBZCPXTIHJBJL-UHFFFAOYSA-N trans-decahydronaphthalene Natural products C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 claims abstract description 12
- NNBZCPXTIHJBJL-MGCOHNPYSA-N trans-decalin Chemical compound C1CCC[C@@H]2CCCC[C@H]21 NNBZCPXTIHJBJL-MGCOHNPYSA-N 0.000 claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims description 42
- 238000004821 distillation Methods 0.000 claims description 28
- 239000001257 hydrogen Substances 0.000 claims description 16
- 229910052739 hydrogen Inorganic materials 0.000 claims description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 229930195733 hydrocarbon Natural products 0.000 claims description 13
- 150000002430 hydrocarbons Chemical class 0.000 claims description 13
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- 239000010779 crude oil Substances 0.000 claims description 9
- 239000004215 Carbon black (E152) Substances 0.000 claims description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 8
- 239000003350 kerosene Substances 0.000 claims description 7
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 6
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 6
- 229910052750 molybdenum Inorganic materials 0.000 claims description 6
- 239000011733 molybdenum Substances 0.000 claims description 6
- 239000003085 diluting agent Substances 0.000 claims description 5
- 229910052759 nickel Inorganic materials 0.000 claims description 5
- PXXNTAGJWPJAGM-VCOUNFBDSA-N Decaline Chemical compound C=1([C@@H]2C3)C=C(OC)C(OC)=CC=1OC(C=C1)=CC=C1CCC(=O)O[C@H]3C[C@H]1N2CCCC1 PXXNTAGJWPJAGM-VCOUNFBDSA-N 0.000 claims description 4
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 4
- 229910000510 noble metal Inorganic materials 0.000 claims description 4
- 229910052697 platinum Inorganic materials 0.000 claims description 4
- PXXNTAGJWPJAGM-UHFFFAOYSA-N vertaline Natural products C1C2C=3C=C(OC)C(OC)=CC=3OC(C=C3)=CC=C3CCC(=O)OC1CC1N2CCCC1 PXXNTAGJWPJAGM-UHFFFAOYSA-N 0.000 claims description 4
- 229910052763 palladium Inorganic materials 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 125000003118 aryl group Chemical group 0.000 claims description 2
- 229910017052 cobalt Inorganic materials 0.000 claims description 2
- 239000010941 cobalt Substances 0.000 claims description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- NNBZCPXTIHJBJL-AOOOYVTPSA-N cis-decalin Chemical compound C1CCC[C@H]2CCCC[C@H]21 NNBZCPXTIHJBJL-AOOOYVTPSA-N 0.000 abstract description 7
- 238000010438 heat treatment Methods 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 150000001336 alkenes Chemical class 0.000 description 13
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 150000001491 aromatic compounds Chemical class 0.000 description 6
- 238000005194 fractionation Methods 0.000 description 6
- 238000005336 cracking Methods 0.000 description 5
- -1 naphthalene trans decalin Chemical compound 0.000 description 5
- 238000011282 treatment Methods 0.000 description 5
- 238000005899 aromatization reaction Methods 0.000 description 3
- 238000003889 chemical engineering Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000010791 quenching Methods 0.000 description 3
- 230000000171 quenching effect Effects 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 238000004517 catalytic hydrocracking Methods 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- 229910052774 Proactinium Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 229910000428 cobalt oxide Inorganic materials 0.000 description 1
- MPMSMUBQXQALQI-UHFFFAOYSA-N cobalt phthalocyanine Chemical compound [Co+2].C12=CC=CC=C2C(N=C2[N-]C(C3=CC=CC=C32)=N2)=NC1=NC([C]1C=CC=CC1=1)=NC=1N=C1[C]3C=CC=CC3=C2[N-]1 MPMSMUBQXQALQI-UHFFFAOYSA-N 0.000 description 1
- IVMYJDGYRUAWML-UHFFFAOYSA-N cobalt(ii) oxide Chemical compound [Co]=O IVMYJDGYRUAWML-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 125000004855 decalinyl group Chemical group C1(CCCC2CCCCC12)* 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002019 disulfides Chemical class 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 150000002790 naphthalenes Chemical class 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910000480 nickel oxide Inorganic materials 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 125000003367 polycyclic group Chemical group 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 239000003380 propellant Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- 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
- C10G69/04—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 step of catalytic cracking in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
Definitions
- the present invention relates to jet fuels, or fuels for jet engines, and their preparation process.
- fuel for jet engines or jet fuels is produced from a fraction of kerosene obtained directly from the atmospheric distillation of crude oil and whose distillation points are between 140 t and 300 ° C and, more typically, between 150 and 270 ° C. This fraction is then either treated in a desulfurization unit, or treated in a unit for converting mercaptans into disulfides.
- Another production route is that consisting of the cracking of a fraction of the distillate under vacuum.
- the fractionation of the effluents makes it possible to obtain a jet fuel which does not require other treatments.
- the jet fuel thus obtained has a very low lubricating power and insufficient for its use in the pure state in jet engines. Therefore, it must be mixed with other jet fuels, in particular direct distillation jet fuels, which have better lubricity and thus compensate for this insufficiency.
- Jet fuels are used to power the burners of aircraft turbojets and propellants.
- jet fuels must have certain characteristics.
- Jet Al jet fuel which is the most commonly used jet fuel in civil aviation, must imperatively have a sulfur content of less than 0.30% by weight, an aromatic compound content of less than 22% by volume, a flash point above 38 ° C, a smoke point above 25 mm, and a defrost point below - 47 ° C.
- jet fuels According to the ways of production of the prior art, jet fuels have similar energy qualities and a lower calorific value whose value is less than 34.60 Mj / liter.
- Jet Al jet fuel Other characteristics of the Jet Al jet fuel are given in Table 6 appearing in the remainder of the present description, after examples of implementation of the invention, this Table 6 also gathering characteristics of the jet fuels produced in these examples.
- the demand for jet fuel is increasing and the means of jet fuel production are limited in a conventional refinery.
- the ydrocracking units are extremely expensive and the quantities of jet fuels produced by the atmospheric distillation of crude oil are limited and depend on the quality of crude oils.
- refineries whose conversion method consists of catalytic cracking only have jet fuels from direct distillation.
- catalytic cracking effluents contain very large quantities of aromatics, olefins, and sulfur products.
- the Applicant has developed a jet fuel characterized in that it has: i) a distillation point in the range from 140 to 300 ° C; ii) a cis decaline / trans decaline ratio greater than 0.2; iii) an aromatic content of less than 22% by volume; iv) a sulfur content of less than 100 ppm; and v) a lower calorific value which is greater than 34.65 Mj / liter.
- the jet fuel according to the invention has a lower calorific value between 34.65 and 35.30 Mj / liter.
- the jet fuel according to the invention is therefore different from the jet fuel of the prior art, in particular as regards its higher calorific value, so that it allows a lower volume consumption than that of the jet fuel of the prior art .
- the invention also aims to provide a new process for the manufacture of this jet fuel with improved properties.
- This process is new and original in that it does not use the conventional ways of producing jet fuel. It thus allows additional production of jet fuel within a refinery, in addition to that produced by the atmospheric distillation cut of crude oil.
- This process makes it possible to obtain a jet fuel from a cut coming from the fractionation of the effluent from a catalytic cracking unit.
- the recovery in jet fuel of a catalytic cracking cut of distillation points between 140 and 300 ° C is possible.
- the catalytic cracking cut is preferably treated in two stages: a hydrotreatment stage and a aromatization stage.
- this catalytic cracking cut has an olefin content of between 20 and 45% and an aromatic compound content of between 40 and 70%, relative to the total volume.
- the specifications of jet fuels limit this aromatics content to a maximum of 22%, which requires dearomatization.
- the dearomatization catalyst is particularly sensitive to pollutants, it is necessary to carry out a hydrotreatment prior to the dearomatization.
- the purpose of the hydrotreatment step is to desulfurize, denitrogenate and hydrogenate the olefins from the catalytic cracking fraction. If the denitrogenation of the charge caused during the ydrotreatment step is weak or insufficient, an additional denitrogenation step will be incorporated into the process diagram.
- the cut resulting from catalytic cracking has properties very different from those which make it possible to obtain jet fuels of the prior art. Thus, it contains more olefins than the cut resulting from direct atmospheric distillation, and further differs from the cut in charge of the cracking which is a vacuum distillate with higher boiling point.
- jet fuel of the invention has characteristics which differ from those of jet fuels obtained by the usual routes.
- the jet fuel according to the invention thus exhibits improved combustion properties in jet engines. Indeed, it comprises a high concentration of polycyclic naphthenes compared to the total concentration of naphthenes of the jet fuel, which results in a gain in substantial energy by volume and greater than 0.5%. Consequently, under identical conditions, the volume consumed of the jet fuel according to the invention will be less than that of a jet fuel of the prior art.
- the jet fuel according to the invention generally has a cis decaline / trans decaline ratio greater than 0.2, and preferably greater than 0.3.
- the catalytic cracking cut from which the jet fuel is derived is rich in olefins, and in particular in dicycloolefins, which are precursors of cis decalin.
- the jet fuel according to the invention also preferably has a naphthalene / trans decaline ratio less than
- the hydrogenation step in accordance with the process according to the invention transforms the vast majority of the naphthalenes present in decalins.
- the jet fuel according to the invention has naphthenes preferably a ratio of between 1.2 and 2. paraffins
- the jet fuel according to the invention has very good quality cold resistance properties and superior to that required for the jet jet fuel Al. Therefore, the jet fuel according to the invention can be advantageously used under severe cold conditions, in particular in the field of military aviation.
- jet fuel of the invention can be mixed with other jet fuel bases, which makes it possible, if necessary, to improve the properties of jet fuel, in particular their energy qualities, while respecting the required standards. for Jet Al jet fuel.
- the hydrotreatment step of the catalytic cracking section is carried out in the presence of a catalyst placed in the form of one or more fixed beds in a reactor.
- the catalyst consists of at least one hydrogenating and / or hydrogenolizing metal deposited on a support substantially neutral, for example catalysts based on nickel and molybdenum such as the catalyst TK 525 from the company Haldor Topsoe or the catalyst HR 348 from the company Procatalyse.
- Other types of catalysts can be used, in particular cobalt and molybdenum catalysts HR 306 and HR 316 from the company Procatalyse, KF 752 from the company Akzo, and TK 524 and TK 554 from the company Haldor Topsoe.
- the reaction temperature is generally between 250 and 350 ° C, under a minimum pressure of 30.105 Pascals (30 bars), with an hourly volume speed of about 1 to 5 hi, the hydrogen / hydrocarbon volume ratio at the inlet of the reactor being between 100 and 500 Mm3 / m3 and preferably between 200 to 300 Nm3 / m3.
- the temperature is around 280 ° C, under a pressure of 35.105 Pascals.
- the hydrotreatment stage generates strongly exothermic reactions.
- a person skilled in the art will adjust various factors, in particular, the temperature at the inlet of the reactor, the hydrogen / hydrocarbons ratio, and the amount of olefins in the feed.
- a diluent such as a reactor recycle or, preferably, kerosene from the atmospheric distillation of crude oil can be optionally mixed with the feed to reduce its concentration of olefins.
- a quenching fluid can be injected between said beds, its nature, its flow rate and its temperature being selected to control the exothermicity of the reactions of this step d 'ydro ⁇ treatment.
- a recycle of the unit, hydrogen or, preferably, kerosene from atmospheric distillation, can constitute the quenching fluid.
- the partial aromatization reaction of the effluent from the desulphurization unit is carried out in the presence of a catalyst, for example in the form of one or several fixed beds in a reactor.
- the catalyst used is selected according to the operating conditions of the reactor.
- the catalyst may be a thioresistant catalyst, consisting of at least one hydrogenating noble metal deposited on a substantially acid support, this noble metal possibly being in particular platinum or palladium.
- thioresistant catalysts such as LD 402 from Procatalyse, AS-100 from Criterion and TK 908 from Haldor Topsoe can be used for this purpose.
- the catalyst used can also be a nickel-based catalyst, which proves to be an advantageous route, since it is more economical than that using catalysts containing platinum or palladium.
- the catalysts such as the catalysts HTC 400 and HTC 500 from Crosfield and C46-7-03 and L3427 from S ⁇ d-Chemie can be used.
- the HTC 400 catalyst from Crosfield is used.
- the reaction temperature is generally between 200 and 300 ° C, under a minimum pressure of 30.105 Pa, with an hourly volume speed of 1 to 5 h -1 , the volume ratio hydrogen / hydrocarbons at the reactor inlet being between 500 and 900 N ⁇ .3 / m3, preferably 600 m3 / m (Nm here means Normal m 3.
- Nm here means Normal m 3.
- 1 Normal m 3 corresponds to lm 3 of gas under standard conditions of temperature and pressure, i.e. 0 ° C and 1 atmosphere - 1.01325.105 Pa).
- the temperature is around 240 ° C, under a pressure of approximately 50.105 pa.
- the reaction temperature is generally between 100 and 200 ° C, under a minimum pressure of 30.105 pa, with an hourly volume speed of 1 to 5 h -1 , the volume ratio hydrogen / hydrocarbons at the reactor inlet being between 600 and 1000 Nm3 / m, preferably equal to 800 Nm 3 / m3.
- the temperature is around 160 ° C, under a pressure of approximately 50.105 pa.
- the catalyst of the dearomatization stage is arranged in several beds, between which a quenching fluid is injected to control the exothermicity of the dearomatization reaction.
- a complementary denitrogenation step can be carried out before that of the daromatization.
- certain dearomatization catalysts are sensitive to nitrogen, which leads to their deactivation. Therefore, if the hydrotreating catalyst selected has not reduced the nitrogen content of the feed sufficiently, it must be treated in order to have a very low nitrogen content of about 10 ppm.
- This treatment can be carried out by various means such as a conventional nitrogen trap containing a denitrogenous mass.
- washing of the effluent from the hydrotreatment stage is necessary in order to remove the ammonia and dissolved hydrogen sulphide which are limiting or poisoning factors for certain types of dearomatization catalysts.
- Example 1 A charge, at distillation points between 150 and 250 ° C, coming directly from the fractionation of a catalytic cracking unit, was treated in accordance with the process according to the invention.
- the load was treated in a hydrotreating unit.
- a catalyst based alumina having a specific surface of 220 m 2 / g, a pore volume of 0.5 cm3 / g, containing, in% by weight, 4.2% of nickel oxide and 16.5% of molybdenum.
- the operation is carried out at an average temperature of 325 ° C. under approximately 35.105 Pa, with an hourly volume speed of 3 hi and a hydrogen / hydrocarbon ratio of 200 m3 / m.
- the catalyst TK 908 from Haldor Topsoe is used for the dearomatization stage.
- the operation is carried out at an average temperature of 240 ° C. under approximately 50.105 Pa, with an hourly volume speed of 1 h-i and one. hydrogen / hydrocarbon ratio of 600 Nm3 / m3.
- Aromatics (% by volume) 45.4 44 7.2
- Olefins (% by volume) 40.3 0 0 naphthenes paraffins - 0.54 1.54 cis decalin trans decalin ._ 0.55 naphthalene trans decalin ⁇ - 0
- the distillation curve is shown in the attached single figure.
- a mass mixture composed of 50% of a kerosene fraction of distillation points between 140 and
- Example 2 A catalyst identical to that of Example 1 is used. The operation is carried out at an average temperature of 300 ° C., under approximately 35.105 p a , with an hourly volume speed of 4 hi and a hydrogen / hydrocarbon ratio of
- the catalyst TK 908 from Haldor Topsoe is used for the dearomatization stage.
- the operation is carried out at an average temperature of 270 ° C., under approximately 50.105 pa, with an hourly volume speed of 3 hi and a hydrogen / hydrocarbon ratio of 600 Nm 3 / m3.
- Aromatic compounds (% by volume) 38 36.1 21
- Olefins (% by volume) 13.9 0 0 naphthenes paraffins - 0.35 0.68 cis decalin trans decalin _ 0.48 naphthalene trans decalin - - 0
- the distillation curve is reproduced in the attached single figure.
- This example illustrates the use of a kerosene fraction resulting from the direct distillation of crude oil as diluent, which makes it possible both to control the exothermicity of the hydrotreatment reactions and to improve the basic qualities of the said fraction. kerosene (especially thawing point and lower calorific value).
- Example 3 A charge at distillation points between 150 and 270 ° C., coming directly from the fractionation of a catalytic cracking unit, was treated in accordance with the process according to the invention.
- the charge was treated in a ydroprocessing unit.
- An alumina catalyst is used having a specific surface of 210 m2 / g, a pore volume of 0.6 cm3 / g, and containing 2.8% of cobalt oxide and 13.8% of molybdenum.
- the operation is carried out at an average temperature of 325 ° C., under approximately 35.105 p a , with an hourly volume speed of 3 hi and a hydrogen / hydrocarbon ratio of 300 Nm.3 / m3.
- the catalyst HTC 400 Crosfield is used for the dearomatization stage. The operation is carried out at an average temperature of 160 ° C. under approximately 50.105 p a , with an hourly volume speed of 3 hi and a hydrogen / hydrocarbon ratio of 800 Nm 3 / m3.
- Aromatic compounds (% by volume) 49 44 21.3
- Olefins (% by volume) 30.7 0.5 0 naphthenes paraffins - 0.60 1.28 cis decalin trans decalin __ - 0.55 naphthalene trans decalin - - 0
- the distillation curve is shown in the attached single figure.
- the operation is carried out in a manner known per se, in the presence of a catalyst based on cobalt phthalocyanine, at a pressure of 8.105 Pa and at a temperature of 50 ° C.
- Aromatic compounds (% by volume) 17.5 17.5
- Olefins (% by volume) 0 0 naphthenes
- the vacuum distillate charge is pretreated in a first reactor in the presence of a denitrogenation catalyst. Then, the effluent obtained is treated in the cracking reactor.
- the operating conditions are substantially similar to those indicated on page 764 of the book “Refining and chemical engineering” by P. Wuithier, IFP, volume 1, 1972 edition.
- Aromatic compounds (% by volume) 52.5 9
- Olefins (% by volume) 0 0 naphthenes
- the distillation curve is shown in the attached single figure.
- the freezing points of Examples 1 and 3 are, in particular, much lower than the minimum required, that is to say less than -47 ° C, and therefore allow potential use of these jet fuels in extreme cold conditions.
- the lower calorific power of the jet fuels obtained according to the invention is particularly high compared to those of the prior art.
Landscapes
- 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)
- Catalysts (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Perforating, Stamping-Out Or Severing By Means Other Than Cutting (AREA)
- Telephone Function (AREA)
- Jet Pumps And Other Pumps (AREA)
Abstract
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9506049A FR2734575B1 (en) | 1995-05-22 | 1995-05-22 | CARBUREACTOR AND PROCESS FOR PREPARING THE SAME |
FR9506049 | 1995-05-22 | ||
PCT/FR1996/000762 WO1996037577A1 (en) | 1995-05-22 | 1996-05-22 | Jet fuel and method for producing same |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0773981A1 true EP0773981A1 (en) | 1997-05-21 |
EP0773981B1 EP0773981B1 (en) | 1999-01-13 |
Family
ID=9479231
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP96917528A Expired - Lifetime EP0773981B1 (en) | 1995-05-22 | 1996-05-22 | Jet fuel and method for producing same |
Country Status (11)
Country | Link |
---|---|
US (1) | US5954941A (en) |
EP (1) | EP0773981B1 (en) |
JP (1) | JP3622771B2 (en) |
AT (1) | ATE175713T1 (en) |
DE (1) | DE69601346T2 (en) |
DK (1) | DK0773981T3 (en) |
ES (1) | ES2126402T3 (en) |
FR (1) | FR2734575B1 (en) |
GR (1) | GR3029514T3 (en) |
WO (1) | WO1996037577A1 (en) |
ZA (1) | ZA964109B (en) |
Families Citing this family (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20070251141A1 (en) * | 2004-02-26 | 2007-11-01 | Purdue Research Foundation | Method for Preparation, Use and Separation of Fatty Acid Esters |
US20050232956A1 (en) * | 2004-02-26 | 2005-10-20 | Shailendra Bist | Method for separating saturated and unsaturated fatty acid esters and use of separated fatty acid esters |
US7892418B2 (en) * | 2005-04-11 | 2011-02-22 | Oil Tech SARL | Process for producing low sulfur and high cetane number petroleum fuel |
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US3175970A (en) * | 1962-03-20 | 1965-03-30 | Gulf Research Development Co | Process for preparing a jet fuel |
US3607729A (en) * | 1969-04-07 | 1971-09-21 | Shell Oil Co | Production of kerosene jet fuels |
US3985638A (en) * | 1974-01-30 | 1976-10-12 | Sun Oil Company Of Pennsylvania | High quality blended jet fuel composition |
FR2268860B1 (en) * | 1974-04-24 | 1977-06-24 | Inst Francais Du Petrole | |
US4409092A (en) * | 1980-04-07 | 1983-10-11 | Ashland Oil, Inc. | Combination process for upgrading oil products of coal, shale oil and crude oil to produce jet fuels, diesel fuels and gasoline |
US4332666A (en) * | 1980-05-06 | 1982-06-01 | Exxon Research & Engineering Co. | Coal liquefaction process wherein jet fuel, diesel fuel and/or ASTM No. 2 fuel oil is recovered |
GB2155034B (en) * | 1983-07-15 | 1987-11-04 | Broken Hill Pty Co Ltd | Production of fuels, particularly jet and diesel fuels, and constituents thereof |
-
1995
- 1995-05-22 FR FR9506049A patent/FR2734575B1/en not_active Expired - Fee Related
-
1996
- 1996-05-22 ES ES96917528T patent/ES2126402T3/en not_active Expired - Lifetime
- 1996-05-22 DK DK96917528T patent/DK0773981T3/en active
- 1996-05-22 ZA ZA964109A patent/ZA964109B/en unknown
- 1996-05-22 US US08/776,170 patent/US5954941A/en not_active Expired - Fee Related
- 1996-05-22 EP EP96917528A patent/EP0773981B1/en not_active Expired - Lifetime
- 1996-05-22 AT AT96917528T patent/ATE175713T1/en not_active IP Right Cessation
- 1996-05-22 JP JP53543596A patent/JP3622771B2/en not_active Expired - Fee Related
- 1996-05-22 DE DE69601346T patent/DE69601346T2/en not_active Expired - Lifetime
- 1996-05-22 WO PCT/FR1996/000762 patent/WO1996037577A1/en active IP Right Grant
-
1999
- 1999-02-26 GR GR990400611T patent/GR3029514T3/en unknown
Non-Patent Citations (1)
Title |
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See references of WO9637577A1 * |
Also Published As
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DK0773981T3 (en) | 1999-08-30 |
DE69601346T2 (en) | 1999-06-17 |
GR3029514T3 (en) | 1999-05-28 |
JPH10503804A (en) | 1998-04-07 |
EP0773981B1 (en) | 1999-01-13 |
DE69601346D1 (en) | 1999-02-25 |
US5954941A (en) | 1999-09-21 |
ATE175713T1 (en) | 1999-01-15 |
ZA964109B (en) | 1996-08-26 |
FR2734575B1 (en) | 1997-08-22 |
JP3622771B2 (en) | 2005-02-23 |
ES2126402T3 (en) | 1999-03-16 |
FR2734575A1 (en) | 1996-11-29 |
WO1996037577A1 (en) | 1996-11-28 |
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