WO2014102287A1 - Procédé pour la préparation de propylène et d'éthylène à partir de gas-oil dérivé de fisher-tropsch - Google Patents

Procédé pour la préparation de propylène et d'éthylène à partir de gas-oil dérivé de fisher-tropsch Download PDF

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Publication number
WO2014102287A1
WO2014102287A1 PCT/EP2013/078000 EP2013078000W WO2014102287A1 WO 2014102287 A1 WO2014102287 A1 WO 2014102287A1 EP 2013078000 W EP2013078000 W EP 2013078000W WO 2014102287 A1 WO2014102287 A1 WO 2014102287A1
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WIPO (PCT)
Prior art keywords
fischer
tropsch derived
gas oil
derived gas
ethylene
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PCT/EP2013/078000
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English (en)
Inventor
Pieter HUIZENGA
Peter LOECKER
Muhammad ZAFAR
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Shell Internationale Research Maatschappij B.V.
Shell Oil Company
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Publication of WO2014102287A1 publication Critical patent/WO2014102287A1/fr

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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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • 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
    • C10G2300/10—Feedstock materials
    • C10G2300/1022—Fischer-Tropsch products
    • 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
    • C10G2400/20—C2-C4 olefins

Definitions

  • the present invention relates to a process for the preparation of propylene and ethylene from a Fischer- Tropsch derived gas oil.
  • Fischer-Tropsch derived products as obtained in a Fischer-Tropsch process as steam cracker feedstock.
  • Fischer-Tropsch derived naphtha comprises paraffins having from 5 to 8 carbon atoms and a boiling range of from 40 to 160°C.
  • a problem of using heavier steam cracker feedstock viz. steam cracker feedstock comprising paraffins having more than 8 carbon atoms and a higher boiling range than 160°C, is that the feedstock may comprise carbon
  • Fischer-Tropsch derived gas oil which Fischer-Tropsch derived gas oil comprises paraffins having from 10 to 35 carbon atoms;
  • step (b) mixing the Fischer-Tropsch derived gas oil provided in step (a) with a dilution gas thereby obtaining a mixture ;
  • step (c) heating the mixture obtained in step (b) thereby
  • step (d) subjecting the mixture obtained in step (c) to a
  • thermal conversion step thereby obtaining a product stream which comprises propylene and ethylene.
  • a heavy steam cracker feedstock comprising Fischer-Tropsch derived product comprising paraffins having from 10 to 35 carbon atoms contain a low amount of carbon residues.
  • Carbon residues are sometimes referred to as compounds with a higher final boiling point than the final boiling point of the steam cracker feedstock. These carbon residues are therefore not evaporated when the stream cracker feedstock is heated to be evaporated prior to being steam cracked.
  • the Fischer-Tropsch derived gas oil according to the present invention can thus be evaporated at a high temperature in an efficient manner with minimal risk of coke formation.
  • a further advantage of the present invention is that due to preheating of the Fischer-Tropsch derived gas oil at a high temperature prior to the thermal conversion of the Fischer-Tropsch derived gas oil, the high temperature at which the thermal conversion takes place, is faster reached. In this way, conversion to propylene and
  • ethylene initiates earlier than when the preheating temperature is much lower than the temperature at which thermal conversion takes place, and results therefore in a high yield of propylene and ethylene.
  • a Fischer-Tropsch derived gas oil comprising paraffins having from 10 to 35 carbon atoms, preferably from 16 to 30 carbon atoms is provided.
  • the Fischer- Tropsch derived gas oil as provided in step (a) is derived from a Fischer-Tropsch process.
  • Fischer-Tropsch derived gas oil is known in the art.
  • Fischer-Tropsch derived is meant that a gas oil, is, or is derived from, a synthesis product of a Fischer-Tropsch process.
  • synthesis gas is converted to a synthesis product.
  • Synthesis gas or syngas is a mixture of hydrogen and carbon monoxide that is obtained by conversion of a hydrocarbonaceous feedstock.
  • Suitable feedstock include natural gas, crude oil, heavy oil fractions, coal, biomass and lignite.
  • a Fischer- Tropsch derived gas oil may also be referred to as a GTL (Gas-to-Liquids ) gas oil.
  • Fischer-Tropsch derived gas oil comprising paraffins having from 10 to 35 carbon atoms as provided in step (a) has been described in e.g. WO 02/070631, WO 02/070629 and in WO 2009/071608.
  • Fischer-Tropsch derived paraffins are primarily n-paraffins .
  • the Fischer-Tropsch derived gas oil according to the present invention comprises more than 90 wt . % of n-paraffins, more
  • n-paraffins preferably more than 95 wt . % of n-paraffins .
  • the Fischer- Tropsch derived gas oil comprises a major amount (i.e. > 50 wt.%) of Fischer-Tropsch derived paraffins having from 10 to 35 carbon atoms; preferably the amount of Fischer- Tropsch paraffins having from 10 to 35 carbon atoms is at least 80 wt.%, more preferably at least 85 wt.%, more preferably at least 90 wt.%, and most preferably at least 95 wt.% based on the total amount of Fischer-Tropsch derived gas oil.
  • the Fischer-Tropsch derived paraffins having from 10 to 35 carbon atoms have typically 50 wt.% of 25 carbon atoms, based on the total amount of Fischer- Tropsch derived paraffins having from 10 to 35 carbon atoms .
  • the Fischer-Tropsch derived gas oil as provided in step (a) has an initial boiling point of at least 300°C, more preferably at least 310°C, most
  • boiling points at atmospheric conditions is meant atmospheric boiling points, which boiling points are determined by ASTM D2887.
  • the Fischer-Tropsch derived gas oil as provided in step (a) has a T10wt.% boiling point from 350 to 380°C, more preferably from 360 to 370°C and a T90wt.% boiling point from 380 to 425°C, and more preferably from 400 to 410°C.
  • T10wt.% is the temperature corresponding to the atmospheric boiling point at which a cumulative amount of 10% of the product is recovered.
  • T90wt.% is the temperature corresponding to the
  • a gas chromatographic method such as ASTM D2887 can be used to determine the level of recovery.
  • the Fischer-Tropsch derived gas oil as provided in step (a) preferably has a density at 20°C (according to ASTM D4052) of at least 700 kg/m 3 , more preferably of at least 750 kg/m 3 and of most 850 kg/m 3 , preferably at most 900 kg/m 3 .
  • step (a) (according to ASTM D445) of the Fischer-Tropsch derived gas oil as provided in step (a) is above 1.5 cSt,
  • the kinematic viscosity at 100°C (according to ASTM D445) of the Fischer-Tropsch derived gas oil as provided in step (a) is below 20 cSt, preferably below 15 cSt, more preferably below 10 cSt, more preferably below
  • the cetane index of the Fischer-Tropsch derived gas oil is in the range of from 75 to 120, preferably in the range from 70 to 80, more preferably in the range from 70 to 75.
  • pour point of the Fischer-Tropsch derived gas oil is preferably below 0°C, more preferably below -10°C, more preferably below -20°C, more preferably below -30°C and most
  • the Fischer-Tropsch derived gas oil has preferably a cloud point according to ASTM D-2500 in the range of -24°C to -34°C, more preferably in the range of -28°C to -32°C.
  • the cold filter plugging point of the Fischer-Tropsch derived gas oil is preferably below 0°C, more preferably below -10°C, more preferably below -15°C, more preferably below -20°C, and most preferably below -30°C and preferably for at most above - 35°C.
  • the Fischer-Tropsch derived gas oil as provided in step (a) is heated to obtain a partly evaporated Fischer-Tropsch derived gas oil.
  • the Fischer-Tropsch derived gas oil is preferably evaporated for at least 80 wt.%, more preferably for at least 90 wt.%.
  • the Fischer-Tropsch derived gas oil as provided in step (a) is heated to at least 150°,
  • the heated Fischer-Tropsch derived gas oil has a temperature of at least 150°C, preferably of at least 195°C.
  • the upper limit of the temperature of the heated Fischer-Tropsch derived gas oil is 430°C.
  • step (a) the heated Fischer-Tropsch derived gas oil is mixed with a dilution gas thereby obtaining a mixture.
  • the Fischer-Tropsch derived gas oil is preferably evaporated for at least 80 wt.% and preferably for at most 90 wt.%.
  • step (b) the Fischer-Tropsch derived gas oil provided in step (a) is mixed with a dilution gas thereby obtaining a mixture.
  • a dilution gas examples include methane, ethane, nitrogen, hydrogen, natural gas, dry gas, refinery off gases, vaporized naphtha and steam.
  • the dilution gas mixed with the Fischer-Tropsch derived gas oil in step (b) comprises steam or hydrogen, more
  • the dilution gas comprises steam.
  • Fischer-Tropsch derived gas oil in step b) is from 0.3 to 0.8, preferably from 0.3 to 0.5, more preferably from 0.3 to 0.45.
  • the temperature of the dilution gas is in the range of 140 to 800°C, preferably in the range of
  • the pressure of dilution gas is not particularly limited. Typically, the pressure of the dilution gas is in the range of 6 to 15 bar.
  • step (c) the mixture as obtained in step (b) is heated thereby obtaining a mixture of diluted gas and an evaporated Fischer-Tropsch derived gas oil.
  • the mixture as obtained in step (b) of the present invention comprises Fischer-Tropsch derived gas oil which is preferably evaporated for at least 95 wt ⁇ 6 , more preferably for at least 99 wt . % and most preferably for at least 100 wt . % .
  • the mixture as obtained in step (c) of the present invention comprises Fischer-Tropsch derived gas oil which is preferably evaporated for at least 95 wt ⁇ 6 , more preferably for at least 99 wt . % and most preferably for at least 100 wt . % .
  • the temperature in step (c) is in the range of from 450 to 650°C, preferably in the range of from 500 to 645°C, more preferably in the range of from 610 to 645°C and most preferably in the range from 610 to 630.
  • the presence of carbon residue in the Fischer-Tropsch derived gas oil according to the present invention leads to coke formation in step (c) .
  • the amount of carbon residue is measured by Micro Carbon Residue Technique (MCRT) according to
  • ASTM D4530 is known in the art and for example described in "Handbook of Petroleum Product Analysis", John Wiley & Sons, Inc., Hoboken, New Jersey, 2002, ISBN 0-471-20346-7, pages 222-223.
  • Fischer-Tropsch derived gasoil samples they need to be pre-thickened . Pre-thickening was accomplished by vacuum distillation in a pot still at a temperature below 250°C. Initial and final amount of sample are weighed.
  • the carbon residue is calculated as final weight divided by initial weight times the measured MCRT.
  • a detection limit of 0.02 wt . % has been demonstrated by first
  • a sample of the Fischer-Tropsch derived gas oil as provided in step (a) comprises less than 10 ppm of carbon residue, more preferably less than 5 ppm of carbon residue, and most preferably less than 2 ppm of carbon residue and at most 20 ppm carbon residue as determined by the method as described above.
  • step (c) Typically the presence of carbon residue in the Fischer-Tropsch derived gas oil according to the present invention leads to coke formation in step (c) .
  • the Fischer-Tropsch derived gas oil as provided in step (a) comprises less than 10 ppmwt of carbon residue, more preferably less than 5 ppmwt of carbon residue, and most preferably less than 2 ppmwt of carbon residue and at most 20 ppmwt carbon residue.
  • the mixture is further heated to a temperature just below the temperature at which thermal conversion starts to occur.
  • This temperature is preferably in the range of from 600 to 650, more preferably in the range of from 610 to 640, and most preferably in the range of from 610 to 630.
  • step (d) the mixture as obtained in step (c) is subjected to a thermal conversion step thereby obtaining a product stream which comprises propylene and ethylene.
  • a thermal conversion step may generally be referred to as a conversion step wherein a "cracking" reaction is performed.
  • a thermal conversion step larger molecules are broken into smaller ones. This can
  • the thermal conversion step is executed as a steam cracking step.
  • Steam cracking is known in the art and therefore not discussed here in detail. Steam cracking is for example described in "Petroleum
  • the temperature in step (d) is in the range of from 700 to 900°C, preferably in the range of from 750 to 850°C, more preferably in the range of from 780 to 830°C.
  • step (d) is generally in the range of from 1 to 3 bar absolute, more preferably from 1.2 to 1.98 bar absolute.
  • step d) the evaporated Fischer-Tropsch derived gas oil of the mixture obtained in step c) is thermally converted to a product stream which comprises propylene and ethylene.
  • step d) the evaporated
  • Fischer-Tropsch derived gas oil of the mixture obtained in step c) is steam cracked to a product stream which comprises propylene and ethylene.
  • Further products of the thermal conversion reaction include, but are not limited to, butadiene, benzene, hydrogen and methane and other associated olefinic, paraffinic, and aromatic products.
  • the product stream comprises from 20 to 35 wt . % ethylene, more preferably, from 25 to 35 wt . % ethylene, and most preferably, from 30 to 35 wt . %
  • step (a) ethylene based on the total amount of Fischer-Tropsch derived gas oil as provided in step (a) .
  • the amount of ethylene is determined by GCxGC- internal test methodology.
  • the product stream comprises from 15 to 25 wt . % propylene, more preferably, from 17 to 25 wt . % propylene, and most preferably, from 18 to 25 wt . % propylene based on the total amount of Fischer-Tropsch derived gas oil as provided in step (a) .
  • the amount of propylene is determined by GCxGC- internal test methodology.
  • the temperature of the product stream in step d) is preferably in the range of from 750 to 850°C, more preferably in the range from 780 to 830°C.
  • the temperature of the product stream of step d) is quickly reduced to terminate any unwanted reactions to a temperature of below 400°C.
  • the product stream is generally cooled by indirect quenching in transfer-line exchangers and or by direct quenching by injection of oil.
  • Transfer-line exchangers and quench oil fitting are known techniques in the art and therefore not discussed here in detail. Transfer-line exchangers and quench oil fittings are for example described in
  • the temperature is reduced to below 400°C by means of a transfer line exchanger and further reduced below 240°C by means of quench oil fitting.
  • step d) Further processing of the cooled product stream of step d) to recover propylene and ethylene is known in the art and therefore not discussed here in detail. Further processing of the product stream including the recovery of propylene and ethylene from the product stream is for example described in "Petroleum Technology", John Wiley & Sons, Inc., and WILEY-CBH verlag GmbH & Co. KGaA,
  • the process of the present invention can be applied in a pyrolysis or cracking furnace.
  • the cracking furnace setup is generally referred to with reference numeral 1.
  • a cracking furnace 1 comprises a
  • convection zone 2 which comprises a feed preheating zone 3, first preheating zone 4, a second preheating zone 5 and a cracking zone 8 (also known as radiant section) .
  • first preheating zone 4 a first preheating zone 4
  • second preheating zone 5 a second preheating zone 5
  • cracking zone 8 also known as radiant section
  • an inlet 6 for dilution gas is located.
  • a stream 10 comprising Fischer-Tropsch derived gas oil comprising paraffins having from 10 to 35 carbon atoms is fed.
  • the pressure and temperature at which the Fischer-Tropsch derived gas oil 10 is fed to the inlet 31 of the feed preheating zone 3 is not critical; typically the
  • the pressure within the feed preheating zone 3 is not particularly limited.
  • the pressure is generally in the range of 4 to 21 bar.
  • the Fischer-Tropsch derived gas oil 10 is heated to obtain a partly evaporated Fischer-Tropsch derived gas oil 11.
  • the heated Fischer-Tropsch derived gas oil 11 as obtained in the feed preheating zone 3 has a temperature of at least 150°C, preferably at least 195°C.
  • the upper limit of the temperature of the heated Fischer- Tropsch derived gas oil 11 as obtained in the first preheating zone 3 is below 400 °C.
  • a dilution gas 12 is added to the inlet 5 of the convection zone.
  • the temperature of the dilution gas 12 at the inlet 6 of the convection zone 2 is in the range of 140 to 800°C, preferably in the range of 150 to 600°C and more preferably in the range of 200 to 550°C.
  • the pressure of dilution gas 12 is not particularly limited, but is preferably sufficient to allow injection at the inlet 6 of the convection zone 2. Typically, the pressure of the dilution gas 12 is in the range of 6 to 15 bar.
  • the heated Fischer-Tropsch derived gas oil 11 as obtained in the feed preheating zone 3 is preferably mixed with the dilution gas 12 at the inlet 6. Typically, the mixture 13 obtained is led to the first preheating zone 4.
  • the heated Fischer-Tropsch derived gas oil 11 as obtained in the feed preheating zone 3 is fed directly to the first preheating zone 4 and mixed with dilution gas 12 in the first preheating zone 4 to obtain a mixture 13.
  • the conditions of the heated Fischer- Tropsch derived gas oil 13 at the inlet 41 of the first preheating zone 4 is similar as the conditions as
  • a dilution gas 14 is added to the inlet 15 of the convection zone.
  • the temperature of the dilution gas 14 at the inlet 15 of the convection zone 2 is in the range of 140 to 800°C, preferably in the range of 150 to 600°C and more preferably in the range of 200 to 550°C.
  • the pressure of dilution gas 14 is not particularly limited, but is preferably sufficient to allow injection at the inlet 15 of the convection zone 2. Typically, the pressure of the dilution gas 14 is in the range of 6 to 15 bar.
  • the heated Fischer-Tropsch derived gas oil 13 as obtained in the feed preheating zone 4 is preferably mixed with the dilution gas 14 at the inlet 15.
  • the mixture 16 obtained is led to the second preheating zone 5.
  • the heated Fischer-Tropsch derived gas oil 13 as obtained in the feed preheating zone 3 is fed directly to the first preheating zone 4 and mixed with dilution gas 14 in the second preheating zone 5 to obtain a mixture 16.
  • the temperature of the heated Fischer- Tropsch derived gas oil 16 at the inlet 51 of the second preheating zone 5 is at least 150°C, preferably of at least 195°C.
  • the mixture 16 is preferably heated further to a temperature just below the temperature at which thermal conversion starts to occur.
  • the temperature in the second preheating zone 5 is in the range of from 450 to 650°C, preferably in the range of from 500 to 645°C, more preferably in the range of from 610 to 645°C and most preferably of from 610 to 630°C.
  • the mixture 17 as obtained in second preheating zone 5 of the convection zone 2 is led to the cracking zone 8 of the cracking furnace 1.
  • the mixture 17 is preferably thermally converted in the cracking zone 8 of the
  • the mixture 17 is steam cracked in the cracking zone 8 of the cracking furnace 1.
  • the temperature in the cracking zone 8 is in the range of from 700 to 900°C, preferably in the range of from 750 to 850°C, more preferably in the range of from 780 to 830°C.
  • the pressure in the cracking zone 8 is generally in the range of from 1 to 3 bar absolute, more preferably from 1.2 to 1.98 bar absolute.
  • the mixture 17 obtained in the second preheating zone 5 is thermally converted to a product stream 18 which comprises propylene and ethylene.
  • the evaporated Fischer- Tropsch derived gas oil of the mixture 17 is steam- cracked to a product stream which comprises propylene and ethylene.
  • Further products of the thermal conversion reaction include, but are not limited to, butadiene, benzene, hydrogen and methane and other associated olefinic, paraffinic, and aromatic products.
  • the temperature of the product stream 18 is
  • the temperature of the product stream 18 is quickly reduced by a transfer-line exchanger 9 to terminate any unwanted reactions to a temperature of below 400°C.
  • the Fischer-Tropsch derived gas oil was obtained by the process as described in Example 1 of WO 02/070629.
  • the properties of the Fischer-Tropsch derived gas oil are listed in Tables 1 and 2.
  • Fischer-Tropsch derived gas oil comprising paraffins having 10 to 35 carbon atoms
  • Fischer-Tropsch derived gas oil comprising paraffins having 10 to 35 carbon atoms
  • helium at a flow rate of between 584-620 Nml/min and nitrogen at a flow rate of between 41.30 Nml/min were pumped to obtain a mixture of Fischer- Tropsch derived gas oil, helium and nitrogen.
  • Helium was used as a dilution gas (in lieu of steam, which is used commercially) , and nitrogen was used as internal standard for the GC .
  • the simulated steam to Fischer-Tropsch derived gas oil ratio was 0.6 on a weight basis.
  • the temperature of the evaporator was increased to 550°C to fully evaporate the Fischer-Tropsch derived gas oil mixture to obtain a mixture comprising evaporated Fischer-Tropsch derived gas oil, helium and nitrogen.
  • This mixture was then transferred to a glass reactor tube (diameter of glass tube was 2mm) .
  • the reactor tube was heated for 0.240 (s) to several high temperatures (see Table 3: Experiments A, B, C, and D) to thermally convert the evaporated Fischer-Tropsch derived gas oil to a product stream comprising propylene and ethylene.
  • the pressure in the tube was 2.25 bar absolute.
  • the product stream was cooled in a series of quench vessels to approximately 96°C.
  • the composition of the product streams obtained in Experiments A, B, C and D was analysed with gas chromatographic method (GCxGC internal testing methodology) and shown in Table 3.
  • MCRT Micro Carbon Residue Technique
  • ASTM D4530 was followed for determining the amount of residue by Micro Carbon Residue Technique (MCRT) .
  • MCRT is for example described in "Handbook of Petroleum Product Analysis", John Wiley & Sons, Inc., Hoboken, New Jersey, 2002, ISBN 0-471-20346-7, pages 222-223 and 278-279.
  • Pre-thickening was accomplished by vacuum distillation in a pot still at a temperature below 250°C.
  • Initial and final amount of sample are weighed.
  • the carbon residue is calculated as final weight divided by initial weight times the measured MCRT.
  • a detection limit of 0.02 wt . % has been demonstrated by first exposing an empty vial to the ASTM D-4530 test procedure, subsequently weighing it and only then adding a weighed amount of test sample. This procedure was applied in the ASTM D-4530 test described in the present application.
  • a pre-thickened sample was shown to have a residue of less than 0.02 wt.%, leading to a residue of less than 3 ppmwt for the Fischer-Tropsch derived gas oil sample.
  • the amount of residue in the Fischer-Tropsch derived gas oil is shown in Table 1.
  • Example 4 The same procedure was performed as for Example 1, with the exception that the reactor tube was heated for 6.5-7 hours to several high temperatures (see Table 4:
  • Fischer-Tropsch derived gas oil ratio of 0.8.

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Abstract

La présente invention concerne un procédé pour la préparation de propylène et d'éthylène, le procédé comprenant au moins les étapes suivantes : (a) fourniture d'un gas-oil dérivé de Fischer-Tropsch, le gas-oil de Fischer-Tropsch comprenant des paraffines comprenant 10 à 35 atomes de carbone ; (b) mélange du gas-oil dérivé de Fischer-Tropsch fourni dans l'étape (a) avec un gaz de dilution, un mélange étant ainsi obtenu ; (c) chauffage du mélange obtenu dans l'étape (b), un mélange de gaz dilué et de gaz-oil dérivé de Fischer-Tropsch évaporé étant ainsi obtenu ; et (d) soumission du mélange obtenu dans l'étape (c) à une étape de conversion thermique, un flux de produit étant ainsi obtenu, qui comprend du propylène et de l'éthylène.
PCT/EP2013/078000 2012-12-28 2013-12-24 Procédé pour la préparation de propylène et d'éthylène à partir de gas-oil dérivé de fisher-tropsch WO2014102287A1 (fr)

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Cited By (1)

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WO2022155035A1 (fr) * 2021-01-18 2022-07-21 Exxonmobil Chemical Patents Inc. Procédés et systèmes de craquage d'hydrocarbures

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US20070249739A1 (en) * 2006-03-30 2007-10-25 Dierickx Jan L M Process for the preparation of propylene and ethylene from a fischer-tropsch synthesis product
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Publication number Priority date Publication date Assignee Title
WO2003062352A2 (fr) * 2002-01-25 2003-07-31 Shell Internationale Research Maatschappij B.V. Procede de preparation d'olefines inferieures par vapocraquage
US20050209495A1 (en) * 2004-03-22 2005-09-22 Mccoy James N Process for steam cracking heavy hydrocarbon feedstocks
US20080045613A1 (en) * 2004-10-08 2008-02-21 Jan Lodewijk Maria Dierickx Process to Prepare Lower Olefins from a Fischer-Tropsch Synthesis Product
WO2007074127A1 (fr) * 2005-12-27 2007-07-05 Shell Internationale Research Maatschappij B.V. Procede de fabrication d’un produit hydrocarbone contenant du soufre
US20070249739A1 (en) * 2006-03-30 2007-10-25 Dierickx Jan L M Process for the preparation of propylene and ethylene from a fischer-tropsch synthesis product

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WO2022155035A1 (fr) * 2021-01-18 2022-07-21 Exxonmobil Chemical Patents Inc. Procédés et systèmes de craquage d'hydrocarbures

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