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EP1194500B1 - Productions d'olefines - Google Patents

Productions d'olefines Download PDF

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Publication number
EP1194500B1
EP1194500B1 EP00940364A EP00940364A EP1194500B1 EP 1194500 B1 EP1194500 B1 EP 1194500B1 EP 00940364 A EP00940364 A EP 00940364A EP 00940364 A EP00940364 A EP 00940364A EP 1194500 B1 EP1194500 B1 EP 1194500B1
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EP
European Patent Office
Prior art keywords
catalyst
feedstock
olefin
olefins
propylene
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German (de)
English (en)
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EP1194500A1 (fr
Inventor
Jean-Pierre Dath
Walter Vermeiren
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Total Petrochemicals Research Feluy SA
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Atofina Research SA
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    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
    • C10G11/04—Oxides
    • C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
    • 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 cracking an olefin-rich hydrocarbon feedstock which is selective towards light olefins in the effluent.
  • olefinic feedstocks from refineries or petrochemical plants can be converted selectively so as to redistribute the olefin content of the feedstock in the resultant effluent.
  • GB-A-1323710 discloses a dewaxing process for the removal of straight-chain paraffins and slightly branched-chain paraffins, from hydrocarbon feedstocks utilising a crystalline silicate catalyst, in particular ZSM-5.
  • US-A-4247388 also discloses a method of catalytic hydrodewaxing of petroleum and synthetic hydrocarbon feedstocks using a crystalline silicate of the ZSM-5 type. Similar dewaxing processes are disclosed in US-A-4284529 and US-A-5614079.
  • the catalysts are crystalline aluminosilicates and the above-identified prior art documents disclose the use of a wide range of Si/Al ratios and differing reaction conditions for the disclosed dewaxing processes.
  • GB-A-2185753 discloses the dewaxing of hydrocarbon feedstocks using a silicalite catalyst.
  • US-A-4394251 discloses hydrocarbon conversion with a crystalline silicate particle having an aluminium-containing outer shell.
  • Silicalite catalysts exist having varying silicon/aluminium atomic ratios and different crystalline forms.
  • EP-A-0146524 and 0146525 in the name of Cosden Technology, Inc. disclose crystalline silicas of the silicalite type having monoclinic symmetry and a process for their preparation. These silicates have a silicon to aluminium atomic ratio of greater than 80.
  • WO-A-97/04871 discloses the treatment of a medium pore zeolite with steam followed by treatment with an acidic solution for improving the butene selectivity of the zeolite in catalytic cracking.
  • EP-A-0305720 discloses the production of gaseous olefins by catalytic conversion of hydrocarbons.
  • EP-B-0347003 discloses a process for the conversion of a hydrocarbonaceous feedstock into light olefins.
  • WO-A-90/11338 discloses a process for the conversion of C 2 -C 12 paraffinic hydrocarbons to petrochemical feedstocks, in particular to C 2 to C 4 olefins.
  • US-A-5043522 and EP-A-0395345 disclose the production of olefins from paraffins having four or more carbon atoms.
  • EP-A-0511013 discloses the production of olefins from hydrocarbons using a steam activated catalyst containing phosphorous and H-ZSM-5.
  • US-A-4810356 discloses a process for the treatment of gas oils by dewaxing over a silicalite catalyst.
  • GB-A-2156845 discloses the production of isobutylene from propylene or a mixture of hydrocarbons containing propylene.
  • GB-A-2159833 discloses the production of a isobutylene by the catalytic cracking of light distillates.
  • Propylene is obtained from FCC units but at a relatively low yield and increasing the yield has proven to be expensive and limited. Yet another route known as metathesis or disproportionation enables the production of propylene from ethylene and butene. Often, combined with a steam cracker, this technology is expensive since it uses ethylene as a feedstock which is at least as valuable as propylene.
  • EP-A-0109059 discloses a process for converting olefins having 4 to 12 carbon atoms into propylene.
  • the olefins are contacted with an alumino-silicate having a crystalline and zeolite structure (e . g . ZSM-5 or ZSM-11) and having a SiO 2 /Al 2 O 3 molar ratio equal to or lower than 300.
  • the specification requires high space velocities of greater than 50kg/h per kg of pure zeolite in order to achieve high propylene yield.
  • the specification also states that generally the higher the space velocity the lower the SiO 2 /Al 2 O 3 molar ratio (called the Z ratio).
  • This specification only exemplifies olefin conversion processes over short periods (e.g. a few hours) and does not address the problem of ensuring that the catalyst is stable over longer periods (e.g. at least 160 hours or a few days) which are required in commercial production. Moreover, the requirement for high space velocities is undesirable for commercial implementation of the olefin conversion process.
  • crystalline silicates of the MFI type are also well known catalysts for the oligomerisation of olefins.
  • EP-A-0031675 discloses the conversion of olefin-containing mixtures to gasoline over a catalyst such as ZSM-5.
  • the operating conditions for the oligomerisation reaction differ significantly from those used for cracking. Typically, in the oligomerisation reactor the temperature does not exceed around 400°C and a high pressure favours the oligomerisation reactions.
  • GB-A-2156844 discloses a process for the isomerisation of olefins over silicalite as a catalyst.
  • US-A-4579989 discloses the conversion of olefins to higher molecular weight hydrocarbons over a silicalite catalyst.
  • US-A-4746762 discloses the upgrading of light olefins to produce hydrocarbons rich in C 5 + liquids over a crystalline silicate catalyst.
  • US-A-5004852 discloses a two-stage process for conversion of olefins to high octane gasoline wherein in the first stage olefins are oligomerised to C 5 + olefins.
  • US-A-5171331 discloses a process for the production of gasoline comprising oligomerising a C 2 -C 6 olefin containing feedstock over an intermediate pore size siliceous crystalline molecular sieve catalyst such as silicalite, halogen stabilised silicalite or a zeolite.
  • US-A-4414423 discloses a multistep process for preparing high-boiling hydrocarbons from normally gaseous hydrocarbons, the first step comprising feeding normally gaseous olefins over an intermediate pore size siliceous crystalline molecular sieve catalyst.
  • US-A-4417088 discloses the dimerising and trimerising of high carbon olefins over silicalite.
  • US-A-4417086 discloses an oligomerisation process for olefins over silicalite.
  • GB-A-2106131 and GB-A-2106132 disclose the oligomerisation of olefins over catalysts such as zeolite or silicalite to produce high boiling hydrocarbons.
  • GB-A-2106533 discloses the oligomerisation of gaseous olefins over zeolite or silicalite.
  • WO98/56740 discloses a process for converting a hydrocarbon feedstock to light olefins, using a zeolite catalyst free of added metal oxides with a hydrogenation/dehydrogenation function.
  • the catalyst is a zeolite such as ZSM5 or ZSM11 (or others) and has an SiO 2 /Al 2 O 3 molar ratio of from 2:1 up to 2000:1.
  • the present invention provides a process for the catalytic cracking of an olefin-rich feedstock which is selective towards light olefins in the effluent, the process comprising contacting a hydrocarbon feedstock containing one or more olefins, with an MEL-type crystalline silicate catalyst, which has been subjected to a steaming step and has a silicon/aluminium atomic ratio of from 150 to 800, at an inlet temperature of from 500 to 600°C, at an olefin partial pressure of from 0.1 to 2 bars and the feedstock being passed over the catalyst at an LHSV of from 10 to 30h -1 , to produce an effluent with an olefin content of lower molecular weight than that of the feedstock.
  • the present invention can thus provide a process wherein olefin-rich hydrocarbon streams (products) from refinery and petrochemical plants are selectively cracked not only into light olefins, but particularly into propylene.
  • the olefin-rich feedstock is passed over an MEL-type crystalline silicate catalyst, with a particular Si/Al atomic ratio and which has been steamed for example at a temperature of at least 300°C for a period of at least 1 hour with a water partial pressure of at least 10kPa.
  • the feedstock may be passed over the catalyst at a temperature ranging between 500 to 600°C, an olefin partial pressure of from 0.1 to 2 bars and an LHSV of from 10 to 30h -1 .
  • the term "silicon/aluminium atomic ratio" is intended to mean the Si/Al atomic ratio of the overall material, which may be determined by chemical analysis.
  • the stated Si/Al ratios apply not just to the Si/Al framework of the crystalline silicate but rather to the whole material.
  • the feedstock may be fed either undiluted or diluted with an inert gas such as nitrogen. In the latter case, the absolute pressure of the feedstock constitutes the partial pressure of the hydrocarbon feedstock in the inert gas.
  • cracking of olefins is performed in the sense that olefins in a hydrocarbon stream are cracked into lighter olefins and selectively into propylene.
  • the feedstock and effluent preferably have substantially the same olefin content by weight.
  • the olefin content of the effluent is within ⁇ 15wt%, more preferably ⁇ 10wt%, of the olefin content of the feedstock.
  • the feedstock may comprise any kind of olefin-containing hydrocarbon stream.
  • the feedstock may typically comprise from 10 to 100wt% olefins and furthermore may be fed undiluted or diluted by a diluent, the diluent optionally including a non-olefinic hydrocarbon.
  • the olefin-containing feedstock may be a hydrocarbon mixture containing normal and branched olefins in the carbon range C 4 to C 10 , more preferably in the carbon range C 4 to C 6 , optionally in a mixture with normal and branched paraffins and/or aromatics in the carbon range C 4 to C 10 .
  • the olefin-containing stream has a boiling point of from around -15 to around 180°C.
  • the hydrocarbon feedstocks comprise C 4 mixtures from refineries and steam cracking units.
  • Such steam cracking units crack a wide variety of feedstocks, including ethane, propane, butane, naphtha, gas oil, fuel oil, etc.
  • the hydrocarbon feedstock may comprises a C 4 cut from a fluidized-bed catalytic cracking (FCC) unit in a crude oil refinery which is employed for converting heavy oil into gasoline and lighter products.
  • FCC fluidized-bed catalytic cracking
  • such a C 4 cut from an FCC unit comprises around 50wt% olefin.
  • the hydrocarbon feedstock may comprise a C 4 cut from a unit within a crude oil refinery for producing methyl tert-butyl ether (MTBE) which is prepared from methanol and isobutene.
  • MTBE methyl tert-butyl ether
  • Such a C 4 cut from the MTBE unit typically comprises around 50wt% olefin.
  • These C 4 cuts are fractionated at the outlet of the respective FCC or MTBE unit.
  • the hydrocarbon feedstock may yet further comprise a C 4 cut from a naphtha steam-cracking unit of a petrochemical plant in which naphtha, comprising C 5 to C 9 species having a boiling point range of from about 15 to 180°C, is steam cracked to produce, inter alia, a C 4 cut.
  • Such a C 4 cut typically comprises, by weight, 40 to 50% 1,3-butadiene, around 25% isobutylene, around 15% butene (in the form of but-1-ene and/or but-2-ene) and around 10% n-butane and/or isobutane.
  • the olefin-containing hydrocarbon feedstock may also comprise a C 4 cut from a steam cracking unit after butadiene extraction (raffinate 1), or after butadiene hydrogenation.
  • the feedstock may yet further alternatively comprise a hydrogenated butadiene-rich C 4 cut, typically containing greater than 50wt% C 4 as an olefin.
  • the hydrocarbon feedstock could comprise a pure olefin feedstock which has been produced in a petrochemical plant.
  • the olefin-containing feedstock may yet further alternatively comprise light cracked naphtha (LCN) (otherwise known as light catalytic cracked spirit (LCCS)) or a C 5 cut from a steam cracker or light cracked naphtha, the light cracked naphtha being fractionated from the effluent of the FCC unit, discussed hereinabove, in a crude oil refinery. Both such feedstocks contain olefins.
  • the olefin-containing feedstock may yet further alternatively comprise a medium cracked naphtha from such an FCC unit or visbroken naphtha obtained from a visbreaking unit for treating the residue of a vacuum distillation unit in a crude oil refinery.
  • the olefin-containing feedstock may comprise a mixture of one or more of the above-described feedstocks.
  • the use of a C 5 cut as the olefin-containing hydrocarbon feedstock in accordance with a preferred process of the invention has particular advantages because of the need to remove C 5 species in any event from gasolines produced by the oil refinery. This is because the presence of C 5 in gasoline increases the ozone potential and thus the photochemical activity of the resulting gasoline. In the case of the use of light cracked naphtha as the olefin-containing feedstock, the olefin content of the remaining gasoline fraction is reduced, thereby reducing the vapour pressure and also the photochemical activity of the gasoline.
  • C 2 to C 4 olefins may be produced in accordance with the process of the invention.
  • the C 4 fraction is very rich in olefins, especially in isobutene, which is an interesting feed for an MTBE unit.
  • C 2 to C 3 olefins are produced on the one hand and C 5 to C 6 olefins containing mainly iso-olefins are produced on the other hand.
  • the remaining C 4 cut is enriched in butanes, especially in isobutane which is an interesting feedstock for an alkylation unit of an oil refinery wherein an alkylate for use in gasoline is produced from a mixture of C 3 and C 5 feedstocks.
  • the C 5 to C 6 cut containing mainly iso-olefins is an interesting feed for the production of tertiary amyl methyl ether (TAME).
  • TAME tertiary amyl methyl ether
  • olefinic feedstocks can be cracked selectively in the presence of an MEL-type catalyst so as to redistribute the olefinic content of the feedstock in the resultant effluent.
  • the catalyst and process conditions are selected whereby the process has a particular yield on an olefin basis towards a specified olefin in the feedstocks.
  • the catalyst and process conditions are chosen whereby the process has the same high yield on an olefin basis towards propylene irrespective of the origin of the olefinic feedstocks for example the C 4 cut from the FCC unit, the C 4 cut from the MTBE unit, the light cracked naphtha or the C 5 cut from the light crack naphtha, etc., This is quite unexpected on the basis of the prior art.
  • the propylene yield on an olefin basis is typically from 30 to 50% based on the olefin content of the feedstock.
  • the yield on an olefin basis of a particular olefin is defined as the weight of that olefin in the effluent divided by the initial total olefin content by weight.
  • the propylene yield on an olefin basis is 40%. This may be contrasted with the actual yield for a product which is defined as the weight amount of the product produced divided by the weight amount of the feed.
  • the paraffins and the aromatics contained in the feedstock are only slightly converted in accordance with the preferred aspects of the invention.
  • the catalyst for the cracking of the olefins comprises a crystalline silicate of the MEL family which may be a zeolite or any other silicate in that family.
  • MEL zeolite is ZSM-11 which is known in the art.
  • Other examples are Boralite D and silicalite-2 as described by the International Zeolite Association (Atlas of zeolite structure types, 1987, Butterworths).
  • the preferred crystalline silicates have pores or channels defined by ten oxygen rings and a high silicon/aluminium atomic ratio.
  • Crystalline silicates are microporous crystalline inorganic polymers based on a framework of X04 tetrahedra linked to each other by sharing of oxygen ions, where X may be trivalent (e . g . Al,B,...) or tetravalent (e.g. Ge, Si,).
  • X may be trivalent (e . g . Al,B,...) or tetravalent (e.g. Ge, Si,).
  • the crystal structure of a crystalline silicate is defined by the specific order in which a network of tetrahedral units are linked together.
  • the size of the crystalline silicate pore openings is determined by the number of tetrahedral units, or, alternatively, oxygen atoms, required to form the pores and the nature of the cations that are present in the pores.
  • Crystalline silicates with the MEL structure possess a bidirectional intersecting straight pore system with straight channels along [100] having pore diameters of 0.53-0.54 nm.
  • the crystalline silicate catalyst has structural and chemical properties and is employed under particular reaction conditions whereby the catalytic cracking readily proceeds. Different reaction pathways can occur on the catalyst. Under the process conditions, having an inlet temperature of around 500 to 600°C, preferably from 520 to 600°C, yet more preferably 540 to 580°C, and an olefin partial pressure of from 0.1 to 2 bars, most preferably around atmospheric pressure, the shift of the double bond of an olefin in the feedstock is readily achieved, leading to double bond isomerisation. Furthermore, such isomerisation tends to reach a thermodynamic equilibrium. Propylene can be, for example, directly produced by the catalytic cracking of hexene or a heavier olefinic feedstock. Olefinic catalytic cracking may be understood to comprise a process yielding shorter molecules via bond breakage.
  • the catalyst preferably has a high silicon/aluminium atomic ratio, greater than about 150, whereby the catalyst has relatively low acidity. Hydrogen transfer reactions are directly related to the strength and density of the acid sites on the catalyst, and such reactions are preferably suppressed so as to avoid the formation of coke during the olefin conversion process, and composition of the olefinic feedstock. Such high ratios reduce the acidity of the catalyst, thereby increasing the stability of the catalyst. Moreover, the use of Si/Al atomic ratios of greater than 150 has been found to increase the propylene selectivity of the catalyst, i . e . to reduce the amount of propane produced. This increases the purity of the resultant propylene. If the Si/Al atomic ratio is above 800, the catalyst has been found to have low activity and stability with respect to the production of propylene by the catalytic cracking process.
  • the catalyst for use in the catalytic cracking process of the present invention is manufactured by steaming an as-synthesised or commercially available crystalline silicate of the MEL-type.
  • the MEL crystalline silicate catalyst for use in the invention most typically comprises a ZSM-11 catalyst which may be synthesised either using diaminooctane as the templating agent and sodium silicate as the silicon source or tetrabutyl phosphonium bromide as the templating agent and a silica sol as the silicon source.
  • the ZSM-11 catalyst may be prepared by mixing sodium silicate with 1,8 diaminooctane together with aluminium sulphate to form a hydrogel which is then allowed to crystallise to form the crystalline silicate.
  • the organic template material is then removed by calcining.
  • the ZSM-11 catalyst is produced by reacting tetrabutyl phosphonium bromide and sodium hydroxide together with the silica sol prepared from colloidal silica. Again, a crystallisation is performed to produce the crystalline silicate and then the product is calcined.
  • the crystalline silicate is subjected to an ion exchange with a salt. Thereafter the material is dried.
  • the crystalline silicate is subjected to ion exchange with ammonium ions, for example by immersing the crystalline silicate in an aqueous solution of NH 4 Cl or NH 4 NO 3 .
  • Such an ion exchange step is desirable if the amount of sodium ions present in the crystalline silicate is so high that a crystalline sodium silicate phase is formed following calcination of the crystalline silicate which would be difficult to remove.
  • the initial crystalline silicate is modified by a steaming process which, without being bound by theory, is believed to reduce the tetrahedral aluminium in the crystalline silicate framework and to convert the aluminium atoms into octahedral aluminium in the form of amorphous alumina.
  • aluminium atoms are chemically removed from the crystalline silicate framework structure to form alumina particles, those particles appear not to migrate and so do not cause partial obstruction of the pores or channels in the framework which would otherwise inhibit the olefinic cracking processes of the present invention.
  • the steaming step has been found to improve significantly the propylene yield, propylene selectivity and catalyst stability in the olefinic catalytic cracking process.
  • the steam treatment is conducted at elevated temperature, preferably in the range of from 425 to 870°C, more preferably in the range of from 540 to 815°C and at atmospheric pressure and at a water partial pressure of from 13 to 200kPa.
  • the steam treatment is conducted in an atmosphere comprising from 5 to 100% steam.
  • the steam treatment is preferably carried out for a period of from 1 to 200 hours, more preferably from 20 hours to 100 hours. As stated above, the steam treatment tends to reduce the amount of tetrahedral aluminium in the crystalline silicate framework, by forming alumina.
  • the catalyst is thereafter calcined, for example at a temperature of from 400 to 800°C at atmospheric pressure for a period of from 1 to 10 hours.
  • the catalyst may be contacted by a complexing agent for aluminium which may comprise an organic acid in an aqueous solution thereof or a salt of such an organic acid or a mixture of two or more such acids or salts.
  • the complexing agent may in particular comprise an amine, such as ethyl diamine tetraacetic acid (EDTA) or a salt thereof, in particular the sodium salt thereof.
  • EDTA ethyl diamine tetraacetic acid
  • the crystalline silicate may be subjected to a second ion exchange step for reducing the sodium content of the crystalline silicate still further, for example by contacting the catalyst with an ammonium nitrate solution.
  • the steamed crystalline silicate, preferably ZSM-11, catalyst may be mixed with a binder, preferably an inorganic binder, and shaped to a desired shape, e.g. extruded pellets.
  • the binder is selected so as to be resistant to the temperature and other conditions employed in the catalyst manufacturing process and in the subsequent catalytic cracking process for the olefins.
  • the binder is an inorganic material selected from clays, silica, metal oxides such as Zr0 2 and/or metals, or gels including mixtures of silica and metal oxides.
  • the binder is preferably alumina-free.
  • binder which is used in conjunction with the crystalline silicate is itself catalytically active, this may alter the conversion and/or the selectivity of the catalyst.
  • Inactive materials for the binder may suitably serve as diluents to control the amount of conversion so that products can be obtained economically and orderly without employing other means for controlling the reaction rate. It is desirable to provide a catalyst having a good crush strength. This is because in commercial use, it is desirable to prevent the catalyst from breaking down into powder-like materials. Such clay or oxide binders have been employed normally only for the purpose of improving the crush strength of the catalyst.
  • a particularly preferred binder for the catalyst of the present invention comprises silica.
  • the relative proportions of the finely divided crystalline silicate material and the inorganic oxide matrix of the binder can vary widely.
  • the binder content ranges from 5 to 95% by weight, more typically from 20 to 50% by weight, based on the weight of the composite catalyst.
  • Such a mixture of crystalline silicate and an inorganic oxide binder is referred to as a formulated crystalline silicate.
  • the catalyst may be formulated into pellets, extruded into other shapes, or formed into a spray-dried powder.
  • the binder and the crystalline silicate catalyst are mixed together by an extrusion process.
  • the binder for example silica
  • the crystalline silicate catalyst material in the form of a gel is mixed with the crystalline silicate catalyst material and the resultant mixture is extruded into the desired shape, for example pellets.
  • the formulated crystalline silicate is calcined in air or an inert gas, typically at a temperature of from 200 to 900°C for a period of from 1 to 48 hours.
  • the binder preferably does not contain any aluminium compounds, such as alumina. This is because as mentioned above the preferred catalyst for use in the invention has a selected silicon/aluminium ratio of the crystalline silicate. The presence of alumina in the binder yields other excess alumina if the binding step is performed prior to the aluminium extraction step. If the aluminium-containing binder is mixed with the crystalline silicate catalyst following aluminium extraction, this re-aluminates the catalyst. The presence of aluminium in the binder would tend to reduce the olefin selectivity of the catalyst, and to reduce the stability of the catalyst over time.
  • the mixing of the catalyst with the binder may be carried out either before or after the steaming step.
  • the various preferred catalysts of the present invention have been found to exhibit high stability, in particular being capable of giving a stable propylene yield over several days, e.g. up to ten days. This enables the olefin cracking process to be performed continuously in two parallel "swing" reactors wherein when one reactor is operating, the other reactor is undergoing catalyst regeneration.
  • the catalyst of the present invention also can be regenerated several times.
  • the catalyst is also flexible in that it can be employed to crack a variety of feedstocks, either pure or mixtures, coming from different sources in the oil refinery or petrochemical plant and having different compositions.
  • the present inventors have discovered that when dienes are present in the olefin-containing feedstock, this can provoke a faster deactivation of the catalyst. This can greatly decrease the yield on an olefin basis of the catalyst to produce the desired olefin, for example propylene, with increasing time on stream.
  • the present inventors have discovered that when dienes are present in the feedstock which is catalytically cracked, this can yield a gum derived from the diene being formed on the catalyst which in turn decreases the catalyst activity. It is desired in accordance with the process of the invention for the catalyst to have a stable activity over time, typically for at least ten days.
  • the feedstock prior to the catalytic cracking of the olefins, if the olefin-containing feedstock contains dienes, the feedstock is subjected to a selective hydrogenation process in order to remove the dienes.
  • the hydrogenation process requires to be controlled in order to avoid the saturation of the mono-olefins.
  • the hydrogenation process preferably comprises nickel-based or palladium-based catalysts or other catalysts which are typically used for first stage pyrolysis gasoline (Pygas) hydrogenation.
  • Pygas first stage pyrolysis gasoline
  • a particularly preferred catalyst is a palladium-based catalyst, supported on, for example, alumina and containing 0.2-0.8wt% palladium based on the weight of the catalyst.
  • the hydrogenation process is preferably carried out at an absolute pressure of from 5 to 50 bar, more preferably from 10 to 30 bar and at an inlet temperature of from 40 to 200°C.
  • the hydrogen/diene weight ratio is at least 1, more preferably from 1 to 5, most preferably around 3.
  • the liquid hourly space velocity (LHSV) is at least 2h -1 , more preferably from 2 to 5h -1 .
  • the dienes in the feedstock are preferably removed so as to provide a maximum diene content in the feedstock of around 0.1% by weight, preferably around 0.05% by weight, more preferably around 0.03% by weight.
  • the process conditions are selected in order to provide high selectivity towards propylene, a stable olefin conversion over time, and a stable olefinic product distribution in the effluent.
  • Such objectives are favoured by the use of a low acid density in the catalyst (i . e . a high Si/Al atomic ratio of greater than 150) in conjunction with a low pressure, a high inlet temperature and a short contact time, all of which process parameters are interrelated and provide an overall cumulative effect ( e . g . a higher pressure may be offset or compensated by a yet higher inlet temperature).
  • the process conditions are selected to disfavour hydrogen transfer reactions leading to the formation of paraffins, aromatics and coke precursors.
  • the process operating conditions thus employ a high space velocity, a low pressure and a high reaction temperature.
  • the LHSV ranges from 10 to 30h -1 .
  • the olefin partial pressure preferably ranges from 0.1 to 2 bars, more preferably from 0.5 to 1.5 bars.
  • a particularly preferred olefin partial pressure is atmospheric pressure ( i . e . 1 bar).
  • the hydrocarbon feedstocks are preferably fed at a total inlet pressure sufficient to convey the feedstocks through the reactor.
  • the hydrocarbon feedstocks may be fed undiluted or diluted in an inert gas, e.g. nitrogen.
  • the total absolute pressure in the reactor ranges from 0.5 to 10 bars.
  • the present inventors have found that the use of a low olefin partial pressure, for example atmospheric pressure, tends to lower the incidence of hydrogen transfer reactions in the cracking process, which in turn reduces the potential for coke formation which tends to reduce catalyst stability.
  • the cracking of the olefins is preferably performed at an inlet temperature of the feedstock of from 500 to 600°C, more preferably from 520 to 600°C, yet more preferably from 540 to 580°C, typically around 560°C to 570°C.
  • the catalytic cracking process can be performed in a fixed bed reactor, a moving bed reactor or a fluidized bed reactor.
  • a typical fluid bed reactor is one of the FCC type used for fluidized-bed catalytic cracking in the oil refinery.
  • a typical moving bed reactor is of the continuous catalytic reforming type. As described above, the process may be performed continuously using a pair of parallel "swing" reactors.
  • the catalyst Since the catalyst exhibits high stability to olefinic conversion for an extended period, typically at least around ten days, the frequency of regeneration of the catalyst is low. More particularly, the catalyst may accordingly have a lifetime which exceeds one year.
  • the reactor effluent is sent to a fractionator and the desired olefins are separated from the effluent.
  • the C 3 cut containing at least 92% propylene, is fractionated and thereafter purified in order to remove all the contaminants such as sulphur species, arsine, etc..
  • the heavier olefins of greater than C 3 can be recycled.
  • olefin-rich streams from refinery or petrochemical plants are cracked into light olefins, in particular propylene.
  • the light fractions of the effluent can contain more than 92% olefins. Such cuts are sufficiently pure to constitute chemical grade olefin feedstocks.
  • the present inventors have found that the propylene yield on an olefin basis in such a process can range from 30 to 50% based on the olefinic content of the feedstock which contains one or more olefins of C 4 or greater.
  • the effluent has a different olefin distribution as compared to that of the feedstock, but substantially the same total olefin content.
  • a ZSM-11 zeolite having an MEL structure was synthesised using diaminooctane as a templating agent and sodium silicate as the silicon source.
  • the catalyst is prepared by mixing the following three solutions A, B and C where solution A comprised 550ml of sodium silicate (27wt%); solution B comprised 17.87g of 1,8 diaminooctane in 522ml of distilled water; and solution C comprised 2.82g of Al 2 (SO 4 ) 3 .18H 2 O and 550ml of distilled water. Solutions A and B were mixed in a 2 litre autoclave and a hydrogel was obtained by slowly adding solution C.
  • the initial pH value of 11.95 was adjusted to a pH of 11 by adding 35ml of sulphuric acid (97wt%). After stirring for 1 hour the crystallisation reaction was performed at 150°C for a period of 2 days in a 2 litre volume stainless steel autoclave, with stirring at a speed of 150 rpm. The resultant product was washed with 10 litres of distilled water, then dried at 110°C for 16 hours, and finally calcined at a temperature of 600°C for a period of 10 hours in order to remove the organic template material.
  • a scanning electron micrograph of the resultant catalyst showed that the ZSM-11 crystals prepared from the sodium silicate were short and ovate-like with dimensions of around 5 microns by 5 to 6 microns.
  • the powder also contained small particles, which could be attributed to crystalline silica, which was identified by an x-ray diffraction spectrum of the material.
  • the x-ray diffraction spectrum exhibits peaks present in MEL-type crystalline silicates with peaks corresponding to small contaminations of dense silicon oxide faces such as quartz and cristobalite.
  • the resultant crystalline silicate was then subjected to ionic exchange by reacting the crystalline silicate in three successive ion exchange reactions for respective periods of 5, 18 and 5 hours by heating the crystalline silicate under reflux with stirring together with a 0.5M ammonium nitrate solution (8.4ml/g zeolite). This ion exchange reduced the sodium content of the crystalline silicate.
  • the material was then dried at a temperature of 110°C for a period of 16 hours.
  • the zeolite was subjected to a steaming step in which the zeolite was loaded into a tubular reactor and flushed with nitrogen.
  • the temperature was increased up to 550°C.
  • a stream of a steam and nitrogen atmosphere containing 72 vol% of steam was passed over the catalyst.
  • the steam treatment was continued for a period of 48 hours.
  • the zeolite was heated under reflux for a period of 18 hours with a 0.06M ethyl diamine tetraacetic acid (EDTA) salt solution of EDTA-Na 2 (4.2ml/g zeolite) and then washed with distilled water.
  • EDTA ethyl diamine tetraacetic acid
  • Such an extraction was employed with the aim of removing extractable aluminium from the catalyst but in fact such an extraction did not occur because of the unavailability of aluminium in the catalyst for such an extraction treatment. This is because the steaming step although removing Al from the silicate framework does not produce such extractable Al.
  • the catalyst was ion-exchanged with a 0.12M NH 4 Cl solution (4.2ml/g zeolite) under reflux for a period of 18 hours.
  • the zeolite was then washed with water to remove excess chlorine.
  • the ZSM-11 catalyst thus obtained was dried at 110°C and then calcined for a period of 3 hours at a temperature of 400°C.
  • the catalyst thus obtained was then employed in an olefinic catalytic cracking process.
  • the catalyst was reduced to grains of 35-45 mesh and 10ml of the grains were loaded into a tubular reactor having an internal diameter of 10mm and a length of 300mm.
  • the reactor cavity was filled with inert granulates of silicon carbide of 2mm particle size.
  • a thermocouple well was placed inside the reactor to measure the temperature profile in the catalyst bed.
  • the reactor was heated up at a rate of 50°C/hour under nitrogen to a temperature of 560°C.
  • a hydrocarbon feed comprising an LCCS feed having the composition of Feed No.
  • the use of the catalyst in accordance with the invention enables selective catalytic cracking of olefins to produce propylene with a high yield and selectivity towards propylene, and with good stability of the catalyst.
  • a ZSM-11 catalyst was synthesised using tetrabutyl phosphonium bromide as the templating agent and a silica sol available in commerce as colloidal silica under the trade designation Ludox HS-40 from the company E.I du Pont de Nemours & Co., Inc. as the silicon source.
  • a silica source contains only a small amount of aluminium.
  • a ZSM-11 zeolite with an Si/Al ratio of 160 was prepared by mixing the following two solutions A and B, solution A comprising 9g of sodium hydroxide, 41.25g of tetrabutyl-phosphonium bromide and 2.74g of Al 2 (SO 4 ) 3 .18A 2 O and solution B comprising 247.5g of colloidal silica available in commerce under the trade designation Ludox HS-40.
  • Solution A was poured into a two litre autoclave and a hydrogel was obtained by slowly adding solution B and 82.5g of distilled water. The pH of the solution was 12.78.
  • the crystallisation reaction was performed at 155°C for a period of 60 hours in a stainless steel autoclave, with the reaction mixture being stirred at a speed of 150 rpm.
  • the product was washed with 10 litres of distilled water, dried at 110°C for 16 hours and then calcined at a temperature of 600°C for a period of 10 hours.
  • the resultant crystalline silicate was subjected to ion exchange by means of a 0.5M ammonium nitrate solution under reflux and stirring in three successive exchange operations having respective periods of 5, 18 and 5 hours.
  • the ion exchange was employed to reduce the sodium content of the crystalline silicate obtained.
  • the ion-exchanged crystallined silicate was then dried at a temperature of 110°C for a period of 16 hours.
  • the catalyst was then subjected to the same steaming, extraction and second ion-exchange reactions as for the crystalline silicate of Example 1.
  • the crystalline silicate thereby obtained was then subjected to the same catalytic cracking process as for Example 1 using a LCCS feedstock having the composition of Feed No. 2 specified in Table 1.
  • the feedstock had been hydrogenated over a hydrogenation catalyst prior to the catalytic cracking process thereby to reduce the diene content of the feed to a value of 0.05wt%.
  • Table 2 and Figures 2a to 2c The results are shown in Table 2 and Figures 2a to 2c.
  • the initial propylene yield was 17wt% and the propylene selectivity is the (i.e. percentage C 3 - /(C 3 - +C 3 ) ratio) of the effluent was high, being 92% at the start of the run to reach a value of 94% after a time on stream of 30 hours.
  • the catalyst had a good stability and the yield on an olefin basis was above 30% after a time on stream of 160 hours.
  • Example 2 the same steps were employed to produce the steamed zeolite as for Example 2 but the zeolite following steaming was not subjected to a subsequent extraction and second ion exchange.
  • the catalyst was dried at a temperature of 110°C for a period of 16 hours.
  • the zeolite crystals thereby obtained were, prior to ion exchange, homogeneous in shape and exhibited elongated ovate-like shapes with dimensions of 1.5-1.7 by 2.2-3.2 microns.
  • the resultant catalyst was subjected to the same catalytic cracking process as for Example 2 employing the same hydrogenated LCCS feedstock as for Example 2.
  • the results are shown in Table 2 and in Figures 3a to 3c. It may be seen that the initial propylene yield was above 17wt% and decreased to reach a value of 14.6wt% after 100 hours on stream.
  • the selectivity for propylene in the C 3 cut was initially around 90% and reached around 93% after 30 hours on stream.
  • the catalyst comprised the same catalyst as that of Example 1 but with the catalyst having being produced in the absence of the steaming step and subsequent extraction and second ion exchange steps.
  • the catalyst was employed under the same process conditions for the catalytic cracking of the same LCCS feedstock as for Example 1 and the results are shown in Table 2 and in Figures 4a to 4c.
  • Example 1 the use of an unsteamed catalyst in accordance with the Comparative Example had a lower initial yield and selectivity and a lower final yield and selectivity for the production of propylene than for Example 1.
  • the initial yield of propylene was around 14wt% and reached 13wt% after 18 hours.
  • the propane production was reasonably high therefore as compared to Example 1. It may thus be concluded from a comparison of Example 1 and Comparative Example 1 that the use of steaming in accordance with the invention greatly increases the selectivity of the catalyst for the production of propylene.
  • a crystalline silicate ZSM-11 catalyst was prepared using a process similar to that employed in Examples 2 and 3, except that the catalyst was not subjected to a steaming step.
  • a ZSM-11 catalyst having an Si/Al atomic ratio of 286 was prepared by mixing two solutions A and B, solution A comprising 9g of sodium hydroxide, 41.25g of tetrabutyl-phosphonium bromide and 1.37g of Al 2 (SO 4 ) 3 .18H 2 O and solution B comprising 247.5g of colloidal silica in the form of Ludox HS-40.
  • Solution A was mixed in a 2 litre autoclave and thereafter a hydrogel was obtained by slowly adding solution B and 82.5g of distilled water.
  • the pH of the solution was 12.8. After stirring for a period of 1 hour, the crystallisation reaction was performed at a temperature of 155°C for a period of 60 hours in a stainless steel autoclave under stirring at a speed of 150rpm. The product was washed with 10 litres of distilled water, dried at 110°C for a period of 16 hours and calcined at a temperature of 600°C for a period of 10 hours in order to remove the organic template material.
  • the resultant crystalline silicate was subject to ion exchange by means of a 0.5M ammonium nitrate solution (8.4ml/g zeolite) under reflux and stirring in three successive reactions for respective periods of 5, 18 and 5 hours in order to reduce the sodium content of the catalyst.
  • the material was then dried at a temperature of 110°C for 16 hours.
  • Example 2 The resultant catalyst was then employed in a catalytic cracking process as for Example 1, the LCCS feedstock having the same composition as for that of Example 1, i.e. Feed No. 1.
  • the results are shown in Table 2 and Figures 5a to 5b.
  • the zeolite employed in Comparative Example 2 had not be subjected to a steaming process but had a higher amount of acid sites than for the earlier Examples and Comparative Examples.
  • the propylene production was initially around 17wt%, with a decrease in activity of around 5wt% after 100 hours on stream.
  • the olefinicity was initially low at less than 86% and after 100 hours on stream was less than 95%.
  • the low olefinicity is believed to be the result of still a too high acid site density.
  • Such a high acid density enhances hydrogen transfer reactions, thereby producing paraffins.
  • the results for Comparative Example 2 show a reasonably good propylene yield and selectivity at the indicated time on stream in Table 2, nevertheless if additionally a steaming process had been employed at such acid density as compared to those employed for Examples 2 and 3, then the propylene yield and selectivity would have been yet higher. It was noted that for Comparative Example 2 the final propylene yield and selectivity are both lower than that for Example 2 and Example 3.
  • an unmodified ZSM-11 catalyst having a very high Si/Al atomic ratio of 843 was prepared as described below.
  • a solution A comprising 9g of sodium hydroxide and 41.25g of tetrabutyl-phosphonium bromide was mixed in a 2 litre autoclave and then a hydrogel was obtained by slowly adding a solution B comprising 247.5g of colloidal silica under the trade designation Ludox HS-40 and 84.5g of distilled water.
  • the pH of the solution was 12.82.
  • the crystallisation reaction was performed at a temperature of 155°C for a period of 60 hours in a stainless steel autoclave under stirring at a speed of 150 rpm.
  • the product was washed by 10 litres of distilled water, dried at 110°C for 16 hours and then calcined at a temperature of 600°C for 10 hours.
  • the crystalline silicate obtained was subjected to ion exchange by means of a 0.5M ammonium nitrate solution (8.4ml/g zeolite) under reflux and stirring in three successive ion exchange operations for respective periods of 5, 18 and 5 hours in order to reduce the sodium content of the crystalline silicate.
  • the synthesised product was then dried at a temperature of 110°C for a period of 16 hours.
  • the thus-obtained catalyst was employed in a catalytic cracking process similar to that employed in Example 1.
  • the feedstock comprised an LCCS having the composition of Feed No. 3 specified in Table 1 and the results are shown in Table 2 and in Figures 6a to 6c.
  • the propylene production was around 15wt% and decreased rapidly to reach 9wt% after 23 hours.
  • the low activation rate was believed to be resultant from the low amount of acid sites found in the zeolite.
  • the propylene yield was low as compared to the Examples of the invention.
  • the ZSM-11 catalyst comprised the same catalyst as that of Example 2 but which had not been subjected to steaming and extraction steps.
  • the catalyst of Comparative Example 4 was subjected to ion exchange with the ammonium nitrate solution as for the catalyst of Example 2, and then dried at 110°C for a period of 16 hours.
  • the as prepared catalyst was then employed in a catalytic cracking process similar to that of Example 1 using the same hydrogenated feed as for Example 2.
  • the results are shown in Table 2 and in Figures 7a to 7c.

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  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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  • Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)

Claims (10)

  1. Procédé pour le craquage catalytique d'une charge riche en oléfines sélectif envers les olêfines légères dans l'effluent, le procédé comprenant la mise en contact de la charge d'hydrocarbure contenant une ou plusieurs oléfines, avec un catalyseur de silicate cristallin MEL, qui a été soumis à une étape de traitement à la vapeur et a un rapport atomique silicium/aluminium de 150 à 800, à une température d'entrée de 500 à 600°C, à une pression partielle d'oléfines de 0,1 à 2 bars et la charge passant sur le catalyseur à une LHSV de 10 à 30h-1, pour produire un effluent ayant une teneur en oléfines à poids moléculaire inférieur à celui de la charge.
  2. Procédé selon la revendication 1, au cours duquel le catalyseur a été traité à la vapeur à une température d'au moins 300°C pendant une période d'au moins 1 heure à une pression partielle d'eau d'au moins 10kPa.
  3. Procédé selon la revendication 1, au cours duquel le catalyseur a été traité à la vapeur à une température de 425 à 870°C, à une pression partielle de vapeur de 13 à 100 kPa pendant une période de 1 à 200 heures.
  4. Procédé selon l'une quelconque les revendications précédentes au cours duquel le catalyseur comprend un catalyseur ZSM-11.
  5. Procédé selon l'une quelconque les revendications précédentes au cours duquel la charge comprend des hydrocarbures en C4 à C10.
  6. Procédé selon l'une quelconque les revendications précédentes au cours duquel l'effluent comprend des composés C3.
  7. Procédé selon la revendication 1, au cours duquel le propylène constitue au moins 92% des composés C3 présents dans l'effluent.
  8. Procédé selon la revendication 6 ou la revendication 7, au cours duquel le craquage catalytique se fait avec un rendement en propylène, basé sur l'oléfine, de 30 à 50% basé sur la teneur en oléfines de la charge.
  9. Procédé selon l'une quelconque des revendications précédentes au cours duquel les teneurs en oléfines en poids de la charge et de l'effluent sont à moins de ±15% l'une de l'autre.
  10. Procédé selon l'une quelconque des revendications précédentes au cours duquel la température d'entrée est de 540 à 580°c.
EP00940364A 1999-06-17 2000-06-08 Productions d'olefines Expired - Lifetime EP1194500B1 (fr)

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EP99111726A EP1061118A1 (fr) 1999-06-17 1999-06-17 Production d' oléfines
EP99111726 1999-06-17
PCT/EP2000/005401 WO2001000749A1 (fr) 1999-06-17 2000-06-08 Productions d'olefines
EP00940364A EP1194500B1 (fr) 1999-06-17 2000-06-08 Productions d'olefines

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Cited By (4)

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US9079813B2 (en) 2010-08-03 2015-07-14 Total Research & Technology Feluy Process to make propylene from isobutanol by dehydration and subsequent cracking
EP3703855A1 (fr) * 2017-11-02 2020-09-09 PTT Global Chemical Public Company Limited Catalyseur pour la production d'oléfines à partir de déshydrogénation d'alcanes et procédé de production d'oléfines à l'aide dudit catalyseur
US11643371B2 (en) 2019-11-22 2023-05-09 Totalenergies Onetech Alkyl halides conversion into ethylene and propylene
US11945760B2 (en) 2019-11-22 2024-04-02 Totalenergies Onetech Process for converting one or more methyl halides into ethylene and propylene

Families Citing this family (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1365004A1 (fr) * 2002-05-23 2003-11-26 ATOFINA Research Production d'olefines
EP1508555A1 (fr) * 2003-08-19 2005-02-23 Total Petrochemicals Research Feluy Procédé de production d'oléfines
WO2009016155A2 (fr) 2007-07-31 2009-02-05 Total Petrochemicals Research Feluy Procédé d'utilisation de tamis moléculaires modifiés par du phosphore visant à convertir des composés organiques en oléfines
EP2082803A1 (fr) 2008-01-25 2009-07-29 Total Petrochemicals Research Feluy Procédé pour l'obtention de composites catalyseurs comprenant du MeAPO et leur utilisation dans la conversion de substances organiques en oléfines
EP2082802A1 (fr) 2008-01-25 2009-07-29 Total Petrochemicals Research Feluy Procédé pour l'obtention d'un composite catalyseur
EP2082801A1 (fr) 2008-01-25 2009-07-29 Total Petrochemicals Research Feluy Processus pour obtenir des tamis moléculaires modifiés
EP2108635A1 (fr) 2008-04-11 2009-10-14 Total Petrochemicals Research Feluy Processus de fabrication d'oléfines à partir d'éthanol
EP2108637A1 (fr) 2008-04-11 2009-10-14 Total Petrochemicals Research Feluy Processus de fabrication d'oléfines à partir d'éthanol
EP2143700A1 (fr) 2008-06-25 2010-01-13 Total Petrochemicals Research Feluy Procédé pour la fabrication d'oléfines à partir de composés oxygénés
EP2336272A1 (fr) 2009-12-15 2011-06-22 Total Petrochemicals Research Feluy Décongestionnement d'une unité de craquage à vapeur pour améliorer la production de propylène
US20130217935A1 (en) 2010-08-03 2013-08-22 Total Research & Technology Feluy Process to make olefins from methanol and isobutanol
US10464053B2 (en) 2011-08-03 2019-11-05 Total Research & Technology Feluy Method for making a catalyst comprising a phosphorous modified zeolite and use of said zeolite
CA2844363C (fr) 2011-08-03 2020-07-14 Total Research & Technology Feluy Catalyseur comprenant une zeolithe modifiee par du phosphore et ayant partiellement une structure alpo
WO2013147218A1 (fr) * 2012-03-30 2013-10-03 Ｊｘ日鉱日石エネルギー株式会社 Zéolite zsm-22, catalyseur d'hydroisomérisation et son procédé de fabrication, et procédé de fabrication d'un hydrocarbure
WO2018210827A1 (fr) 2017-05-17 2018-11-22 Total Research & Technology Feluy Procédé de valorisation de mto-ocp pour maximiser la sélectivité en propylène
WO2021198166A1 (fr) 2020-03-30 2021-10-07 Total Se Procédé de conversion de gaz en oléfines avec coproduction d'hydrogène conjointement à un procédé d'intégration thermique
WO2021198175A1 (fr) 2020-03-30 2021-10-07 Total Se Procédé de conversion de gaz en oléfines avec coproduction d'hydrogène conjointement avec une section de réaction électrifiée
EP4397790A3 (fr) 2020-03-30 2024-10-30 TotalEnergies OneTech Procédés de production d'hydrogène par gaz en oléfines
WO2021198479A1 (fr) 2020-04-03 2021-10-07 Total Se Production d'oléfines légères par oxychloration

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3372474D1 (en) * 1982-11-10 1987-08-20 Montedipe Spa Process for converting olefins having 4 to 12 carbon atoms into propylene
WO1998056740A1 (fr) * 1997-06-10 1998-12-17 Exxon Chemical Patents Inc. Systeme multireacteur de production amelioree d'olefines legeres
EP0921179A1 (fr) * 1997-12-05 1999-06-09 Fina Research S.A. Production d'oléfines

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9079813B2 (en) 2010-08-03 2015-07-14 Total Research & Technology Feluy Process to make propylene from isobutanol by dehydration and subsequent cracking
EP3703855A1 (fr) * 2017-11-02 2020-09-09 PTT Global Chemical Public Company Limited Catalyseur pour la production d'oléfines à partir de déshydrogénation d'alcanes et procédé de production d'oléfines à l'aide dudit catalyseur
US11643371B2 (en) 2019-11-22 2023-05-09 Totalenergies Onetech Alkyl halides conversion into ethylene and propylene
US11945760B2 (en) 2019-11-22 2024-04-02 Totalenergies Onetech Process for converting one or more methyl halides into ethylene and propylene

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PT1194500E (pt) 2003-12-31
WO2001000749A1 (fr) 2001-01-04
AU5532300A (en) 2001-01-31
DE60004367T2 (de) 2004-08-05
EP1194500A1 (fr) 2002-04-10
ATE246720T1 (de) 2003-08-15
EP1061118A1 (fr) 2000-12-20
ES2203487T3 (es) 2004-04-16
DE60004367D1 (de) 2003-09-11
JP2001031980A (ja) 2001-02-06

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