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WO2017115231A1 - Procédé de traitement d'alpha-oléfines linéaires - Google Patents

Procédé de traitement d'alpha-oléfines linéaires Download PDF

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Publication number
WO2017115231A1
WO2017115231A1 PCT/IB2016/057886 IB2016057886W WO2017115231A1 WO 2017115231 A1 WO2017115231 A1 WO 2017115231A1 IB 2016057886 W IB2016057886 W IB 2016057886W WO 2017115231 A1 WO2017115231 A1 WO 2017115231A1
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WO
WIPO (PCT)
Prior art keywords
reactor
linear alpha
stream
droplets
alpha olefins
Prior art date
Application number
PCT/IB2016/057886
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English (en)
Inventor
Haresh PATEL
Suprayudi S. KADIR
Original Assignee
Sabic Global Technologies B.V.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sabic Global Technologies B.V. filed Critical Sabic Global Technologies B.V.
Publication of WO2017115231A1 publication Critical patent/WO2017115231A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
    • C07C2/08—Catalytic processes

Definitions

  • linear alpha olefins A major portion of the petrochemical industry is concerned with the production and use of linear alpha olefins.
  • C4-C8 linear alpha olefins can be used as comonomer in the production of polyethylene.
  • C14 can be converted to chloroparaffins or used as an on-land drilling fluid.
  • C16-C18 linear alpha olefins can be used as the hydrophobic material in oil-soluble surfactants. Therefore, the production of linear alpha olefins remains an important goal of the petrochemical industry.
  • Linear alpha olefins can be produced by the oligomerization of ethylene.
  • Bubble column reactors are widely known.
  • a bubble column reactor is, for example, utilized for the oligomerization of ethylene to form linear alpha-olefins (LAO).
  • LAO linear alpha-olefins
  • Such a bubble column reactor comprises a column reactor which is divided by a sparger plate into an upper reaction compartment and a bottom compartment. Via the bottom compartment a gaseous feed of monomer(s) is introduced into the column reactor and passes through the sparger plate and into the homogenous solution comprising monomer(s), solvent and catalyst in the upper compartment to then form linear alpha-olefins. From the top of the upper reaction compartment gaseous products and the like are removed. Further, a line is provided to remove a liquid mixture comprising solvent, catalyst, dissolved monomer(s) and linear alpha-olefins.
  • a method of processing linear alpha olefins comprises: passing a feed stream comprising gaseous linear alpha olefins through a reactor; passing the feed stream through a liquid within the reactor to produce a reaction stream, wherein the reaction stream comprises linear alpha olefins, polymer droplets, and linear alpha olefin droplets; and passing the reaction stream through a filter to produce a gaseous product stream that exits the reactor, wherein the gaseous product stream is free of droplets having a diameter of greater than 40 micrometers.
  • a method of processing linear alpha olefins comprises: passing a feed stream comprising gaseous linear alpha olefins through a bubble column reactor; passing the feed stream through a liquid within the bubble column reactor, wherein an oligomerization reaction occurs producing a reaction stream; wherein the liquid comprises linear alpha olefins with greater than or equal to 4 carbon atoms and wherein the reaction stream comprises linear alpha olefins, polymer droplets, and linear alpha olefin droplets; passing the reaction stream through a vane type mist eliminator to produce a gaseous product stream, wherein the gaseous product stream is free of droplets having a diameter of greater than 40 micrometers; passing the gaseous product stream through a condenser within the bubble column reactor; and withdrawing the gaseous product stream from the bubble column reactor.
  • FIG. 1 is a simplified schematic diagram of a linear alpha olefin processing method in accordance with the present disclosure.
  • the method disclosed herein can provide a linear alpha olefin processing method that can effectively and efficiently produce linear alpha olefins without reactor fouling and downstream equipment disruption caused by droplet formation.
  • the method disclosed herein can produce a gaseous product stream that is free of polymer droplets and linear alpha olefin droplets having a size (e.g., diameter) of greater than or equal to 20 micrometers, for example, greater than or equal to 30 micrometers, for example, greater than or equal to 40 micrometers, for example, greater than or equal to 50 micrometers.
  • the method disclosed herein can retain polymer droplets and linear alpha olefin droplets within an oligomerization reactor.
  • the method disclosed herein can prevent the fouling of a reactor used to produce linear alpha olefins.
  • the method disclosed herein can prevent the fouling of a condenser within the reactor caused by polymer droplets and linear alpha olefin droplets.
  • the method disclosed herein can reduce reactor fouling by greater than 50%.
  • the method described herein can also prevent the clogging and disruption of downstream equipment such as piping and heat exchangers caused by the escape of droplets from the reactor. As a result, the method disclosed herein the frequent cleaning, maintenance, and shutdown periods that are required by other methods can be reduced.
  • the method disclosed herein can also provide a linear alpha olefin processing method that is more cost efficient and wherein reactor runtimes are significantly longer than in other methods.
  • the method disclosed herein for processing linear alpha olefins can include passing a feed stream comprising gaseous linear alpha olefins through a bubble column reactor.
  • the feed stream can then be passed through a liquid within the bubble column reactor, wherein an oligomerization reaction can occur thereby producing a reaction stream.
  • the liquid can comprise linear alpha olefins with greater than or equal to 4 carbon atoms.
  • the reaction stream can comprise linear alpha olefins, polymer droplets, and linear alpha olefin droplets.
  • the reaction stream can then be passed through a vane type mist eliminator to produce a gaseous product stream.
  • the gaseous product stream can be free of both polymer droplets and linear alpha olefin droplets having a size (e.g., diameter) of greater than or equal to 20 micrometers, for example, greater than or equal to 30 micrometers, for example, greater than or equal to 40 micrometers, for example, greater than or equal to 50 micrometers.
  • the method disclosed herein can also include passing the gaseous product stream through a condenser within the bubble column reactor. The gaseous product stream can then be withdrawn from the bubble column reactor. The gaseous product stream can also be passed through additional downstream processing units subsequent to withdrawal from the bubble column reactor.
  • the additional downstream processing units can include a condenser, a heat exchanger, a reactor, or a combination comprising at least one of the foregoing.
  • the method disclosed herein for processing linear alpha olefins can include a feed stream.
  • the feed stream can comprise hydrocarbons, linear alpha olefins, or a combination comprising at least one of the foregoing.
  • the feed stream can comprise ethylene, ethane, methane, 1-butene, 1-hexene, 1-octene, or a combination comprising at least one of the foregoing.
  • the feed stream can be in a gaseous phase.
  • the feed stream can comprise gaseous ethylene.
  • the method described herein for processing linear alpha olefins can include passing a feed stream through a reactor.
  • the reactor can be a bubble column reactor.
  • the reactor can be a bubble column reactor for oligomerization.
  • the reactor can comprise steel, other metals, polymers, ceramics, or a combination comprising at least one of the foregoing.
  • a temperature within the reactor can be greater than or equal to 50°C.
  • a temperature within the reactor can be 50°C to 100°C.
  • a pressure within the reactor can be greater than or equal to 2000 kiloPascals.
  • a pressure within the reactor can be 2000 kiloPascals to 3500 kiloPascals.
  • the method disclosed herein for processing linear alpha olefins can include passing a feed stream through a gas distributor and a sparger plate within a reactor.
  • the gas can disperse the feed stream evenly throughout the reactor.
  • the gas can evenly disperse a gaseous ethylene feed stream throughout a bubble column reactor.
  • the reactor can comprise steel, other metals, polymers, ceramics, or a combination comprising at least one of the foregoing.
  • the method disclosed herein for processing linear alpha olefins can include passing a feed stream through a liquid within a reactor.
  • a gaseous feed stream can rise up through the liquid.
  • the liquid can comprise linear alpha olefins.
  • the liquid can comprise linear alpha olefins with greater than or equal to 4 carbon atoms.
  • the liquid can comprise a solvent.
  • the solvent can comprise toluene.
  • the solvent can be introduced to the reactor through a solvent injection stream located in the reactor.
  • the liquid can comprise a catalyst.
  • the liquid can comprise an oligomerization catalyst.
  • the liquid can comprise a zirconium catalyst, an aluminum catalyst, or a combination comprising at least one of the foregoing.
  • the method disclosed herein can include an oligomerization reaction that occurs within a liquid.
  • the oligomerization of ethylene can occur within the liquid.
  • the oligomerization reaction can produce a reaction stream that rises up out of the liquid within the reactor.
  • the reaction stream can comprise droplets produced by the oligomerization reaction.
  • the reaction stream can comprise polymer droplets, linear alpha olefin droplets, or a combination comprising at least one of the foregoing.
  • the reaction stream can comprise polyethylene droplets, linear alpha olefin droplets with greater than or equal to 18 carbon atoms, or a combination comprising at least one of the foregoing with droplet size of 1 micrometer to 100 micrometer.
  • the method disclosed herein for processing linear alpha olefins can include passing the reaction stream through a filter.
  • the filter can be a vane type mist eliminator.
  • the filter can comprise stainless steel, nickel-based alloys, titanium, aluminum, copper, polypropylene, fluoroplastics, glass fibers, or a combination comprising at least one of the foregoing.
  • the filter can comprise a grid arrangement, a knitted arrangement, or a combination comprising at least one of the foregoing.
  • the filter can remove all droplets with more than 40 micrometer & substantially remove lower size droplets from the stream and retain them within the reactor.
  • the filter can produce a gaseous product stream.
  • the gaseous product stream can comprise linear alpha olefins.
  • the gaseous product stream can comprise linear alpha olefins with greater than or equal to 4 carbon atoms.
  • the gaseous product stream can comprise linear alpha olefins with 14 to 18 carbon atoms.
  • the gaseous product stream can comprise hydrocarbons.
  • the gaseous product stream can comprise ethylene, methane, ethane, or a combination comprising at least one of the foregoing.
  • the gaseous product stream can be free of droplets.
  • the gaseous product stream can comprise less than 1% droplets having a size of more than 40 micrometers.
  • the gaseous stream can comprise of 0% droplets having a size of more than 40 micrometers.
  • the method disclosed herein for processing linear alpha olefins can include passing a gaseous product stream through additional downstream processing units subsequent to withdrawal from a reactor.
  • the additional downstream processing units can include a condenser, a heat exchanger, a reactor, or a combination comprising at least one of the foregoing.
  • a gaseous product comprising linear alpha olefins can be used in a variety of applications subsequent to withdrawal from the reactor.
  • C4-C8 linear alpha olefins can be used as comonomer in the production of polyethylene.
  • C14 can be converted to chloroparaffins or used as an on-land drilling fluid.
  • C14 drilling fluid is significantly more biodegradable, less irritating to skin, and less toxic than traditional diesel or kerosene drilling fluid.
  • C16-C18 linear alpha olefins can be used as the hydrophobic material in oil-soluble surfactants.
  • the method disclosed herein can include converting a product from the reactor to chloroparaffin, using a product from the reactor as drilling fluid, or a combination comprising at least one of the foregoing.
  • 1-Hexene is commonly manufactured by two general routes: (i) full-range processes via the oligomerization of ethylene and (ii) on-purpose technology.
  • 1-hexene Prior to the 1970s, 1-hexene was also manufactured by the thermal cracking of waxes. Linear internal hexenes were manufactured by chlorination/dehydrochlorination of linear paraffins.
  • Ethylene oligomerization combines ethylene molecules to produce linear alpha- olefins of various chain lengths with an even number of carbon atoms. This approach results in a distribution of alpha-olefins. Oligomerization of ethylene can produce 21 percent 1-hexene.
  • Fischer-Tropsch synthesis to make fuels from synthesis gas derived from coal can recover 1-hexene from the aforementioned fuel streams, where the initial 1-hexene concentration cut can be 60% in a narrow distillation, with the remainder being vinylidenes, linear and branched internal olefins, linear and branched paraffins, alcohols, aldehydes, carboxylic acids, and aromatic compounds.
  • the trimerization of ethylene by homogeneous catalysts has been demonstrated.
  • linear alpha olefins There are a wide range of applications for linear alpha olefins.
  • the lower carbon numbers, 1-butene, 1-hexene and 1-octene can be used as comonomers in the production of polyethylene.
  • High density polyethylene (HDPE) and linear low density polyethylene (LLDPE) can use approximately 2-4% and 8-10% of comonomers, respectively.
  • C4-C8 linear alpha olefins can be for production of linear aldehyde via oxo synthesis (hydroformylation) for later production of short-chain fatty acid, a carboxylic acid, by oxidation of an intermediate aldehyde, or linear alcohols for plasticizer application by hydrogenation of the aldehyde.
  • An application of 1-decene is in making polyalphaolefin synthetic lubricant basestock (PAO) and to make surfactants in a blend with higher linear alpha olefins.
  • PAO polyalphaolefin synthetic lubricant basestock
  • C 1 0-C 1 4 linear alpha olefins can be used in making surfactants for aqueous detergent formulations. These carbon numbers can be reacted with benzene to make linear alkyl benzene (LAB), which can be further sulfonated to linear alkyl benzene sulfonate (LABS), a popular relatively low cost surfactant for household and industrial detergent applications.
  • LAB linear alkyl benzene
  • LABS linear alkyl benzene sulfonate
  • CM has other applications such as being converted into chloroparaffins.
  • a recent application of CM is as on-land drilling fluid basestock, replacing diesel or kerosene in that application.
  • CM is more expensive than middle distillates, it has a significant advantage environmentally, being much more biodegradable and in handling the material, being much less irritating to skin and less toxic.
  • Ci6 - Ci8 linear olefins find their primary application as the hydrophobes in oil- soluble surfactants and as lubricating fluids themselves.
  • Ci6 - Cis alpha or internal olefins are used as synthetic drilling fluid base for high value, primarily off-shore synthetic drilling fluids.
  • the preferred materials for the synthetic drilling fluid application are linear internal olefins, which are primarily made by isomerizing linear alpha-olefins to an internal position. The higher internal olefins appear to form a more lubricious layer at the metal surface and are recognized as a better lubricant.
  • Another application for Ci6 - Cis olefins is in paper sizing. Linear alpha olefins are, once again, isomerized into linear internal olefins are then reacted with maleic anhydride to make an alkyl succinic anhydride (ASA), a popular paper sizing chemical.
  • ASA alky
  • C20 - C30 linear alpha olefins production capacity can be 5-10% of the total production of a linear alpha olefin plant. These are used in a number of reactive and non-reactive applications, including as feedstocks to make heavy linear alkyl benzene (LAB) and low molecular weight polymers used to enhance properties of waxes.
  • LAB linear alkyl benzene
  • 1-hexene can be as a comonomer in production of polyethylene.
  • High- density polyethylene (HDPE) and linear low-density polyethylene (LLDPE) use approximately 2-4% and 8-10% of comonomers, respectively.
  • Heptanal can be converted to the short-chain fatty acid heptanoic acid or the alcohol heptanol.
  • FIG. A more complete understanding of the components, processes, and apparatuses disclosed herein can be obtained by reference to the accompanying drawings.
  • FIG. These figures (also referred to herein as "FIG.") are merely schematic representations based on convenience and the ease of demonstrating the present disclosure, and are, therefore, not intended to indicate relative size and dimensions of the devices or components thereof and/or to define or limit the scope of the exemplary embodiments.
  • specific terms are used in the following description for the sake of clarity, these terms are intended to refer only to the particular structure of the embodiments selected for illustration in the drawings, and are not intended to define or limit the scope of the disclosure.
  • FIG. In the drawings and the following description below, it is to be understood that like numeric designations refer to components of like function.
  • this schematic represents linear alpha olefin processing method 10 in accordance with the present disclosure.
  • the method disclosed herein can include passing a feed stream 14 through a reactor 12.
  • the feed stream 14 can comprise gaseous ethylene and the reactor 12 can be a bubble column reactor.
  • the feed stream 14 can then be passed through a gas distributor 16.
  • the feed stream 14 can then be passed through a sparger plate 18.
  • the gas distributor 16 and the sparger plate 18 can disperse the gaseous ethylene feed stream 14 evenly throughout the reactor 12.
  • the method disclosed herein for processing linear alpha olefins can then include passing the feed stream 14 through a liquid 20.
  • gaseous ethylene can rise up through the liquid 20 within the reactor 12.
  • the liquid 20 can comprise linear alpha olefins, toluene solvent, and a catalyst.
  • catalyst can enter the reactor 12 through the catalyst injection stream 23.
  • Toluene solvent can enter the reactor 12 through solvent injection stream 21.
  • a reaction can occur as the feed stream 14 passes through the liquid 20.
  • an oligomerization reaction can occur producing a reaction stream 22 that rises up out of the liquid 20.
  • the reaction stream can comprise polymer droplets and linear alpha olefin droplets.
  • the method disclosed herein for the processing of linear alpha olefins can then include passing the reaction stream 22 through a filter 28.
  • the filter 28 can be a vane type mist eliminator.
  • the filter 28 can then produce a gaseous product stream 30.
  • the gaseous product stream 30 can be free of polymer droplets and linear alpha olefin droplets have a size of more than 40 micrometers in diameter.
  • the stream 30 can contain a lower concentration of less than 40 micrometers diameter droplets compared to stream 28.
  • the method disclosed herein for the processing linear alpha olefins can then include passing the gaseous product stream 30 through a condenser 34 within the reactor 12.
  • the gaseous product 30 can then be removed from the reactor 12 through the product removal stream 36.
  • the product removal stream 36 can comprise ethylene and linear alpha olefins.
  • the product removal stream 36 can then be further processed by downstream units.
  • additional downstream processing units can include condensers, heat exchangers and reactors.
  • Embodiment 1 A method of processing linear alpha olefins, comprising: passing a feed stream comprising gaseous linear alpha olefins through a reactor; passing the feed stream through a liquid within the reactor to produce a reaction stream, wherein the reaction stream comprises linear alpha olefins, polymer droplets, and linear alpha olefin droplets; and passing the reaction stream through a filter to produce a gaseous product stream that exits the reactor, wherein the gaseous product stream is free of droplets having a diameter of greater than 40 micrometers.
  • Embodiment 2 The method of Embodiment 1, wherein a diameter of the droplets within the agglomerate stream is greater than or equal to 1 micrometer.
  • Embodiment 3 The method of any of the preceding embodiments, wherein the feed stream comprises ethylene gas, ethane gas, methane gas, linear alpha olefins with greater than or equal to 4 carbon atoms, or a combination comprising at least one of the foregoing.
  • Embodiment 4 The method of any of the preceding embodiments, wherein the reactor is a bubble column reactor.
  • Embodiment 5 The method of any of the preceding embodiments, wherein the reactor is an oligomerization reactor.
  • Embodiment 6 The method of any of the preceding embodiments, wherein the liquid comprises linear alpha olefins with greater than or equal to 4 carbon atoms.
  • Embodiment 7 The method of any of the preceding embodiments, wherein the reaction stream comprises polyethylene droplets, linear alpha olefin droplets with greater than or equal to 4 carbon atoms, or a combination comprising at least one of the foregoing.
  • Embodiment 8 The method of any of the preceding embodiments, wherein the filter is a vane type mist eliminator.
  • Embodiment 9 The method of any of the preceding embodiments, further comprising passing the gaseous product stream through an additional downstream processing unit subsequent to exiting the reactor.
  • Embodiment 10 The method of Embodiment 9, wherein the additional downstream processing unit comprises a condenser, a heat exchanger, a reactor, or a combination comprising at least one of the foregoing.
  • Embodiment 11 The method of any of the preceding embodiments, further comprising passing the gaseous product stream through an internal condenser prior to exiting the reactor.
  • Embodiment 12 The method of any of the preceding Embodiments, wherein a temperature within the reactor is greater than or equal to 50°C and a pressure within the reactor is greater than or equal to 2000 kiloPascals.
  • Embodiment 13 The method of any of the preceding embodiments, wherein fouling of the reactor is reduced by greater than 50% as compared to a reactor operated by a different method.
  • Embodiment 14 A method of processing linear alpha olefins, comprising:
  • Embodiment 15 The method of Embodiment 14, further comprising passing the gaseous product stream through an additional downstream processing unit.
  • Embodiment 16 The method of Embodiment 15, wherein the additional downstream processing unit comprises a condenser, a heat exchanger, a reactor, or a combination comprising at least one of the foregoing.
  • Embodiment 17 The method of any of Embodiments 14-16, wherein a diameter of the droplets within the agglomerate stream is greater than or equal to 1 micrometers.
  • Embodiment 18 The method of any of Embodiments 14-17, wherein a temperature within the reactor is greater than or equal to 50°C and a pressure within the reactor is greater than or equal to 2000 kiloPascals.
  • Embodiment 19 A system, comprising: a reactor configured to process linear alpha olefins according to the method of any of Embodiments 1-18.
  • the invention may alternately comprise, consist of, or consist essentially of, any appropriate components herein disclosed.
  • the invention may additionally, or alternatively, be formulated so as to be devoid, or substantially free, of any components, materials, ingredients, adjuvants or species used in the prior art compositions or that are otherwise not necessary to the achievement of the function and/or objectives of the present invention.
  • the endpoints of all ranges directed to the same component or property are inclusive and independently combinable (e.g., ranges of "less than or equal to 25 wt , or 5 wt% to 20 wt ,” is inclusive of the endpoints and all intermediate values of the ranges of "5 wt% to 25 wt ,” etc.).
  • each of the foregoing groups can be unsubstituted or substituted, provided that the substitution does not significantly adversely affect synthesis, stability, or use of the compound.
  • substituted means that at least one hydrogen on the designated atom or group is replaced with another group, provided that the designated atom's normal valence is not exceeded.
  • two hydrogens on the atom are replaced.
  • Exemplary groups that can be present on a "substituted" position include, but are not limited to, cyano; hydroxyl; nitro; azido; alkanoyl (such as a C2-6 alkanoyl group such as acyl); carboxamido; Ci-6 or C 1 -3 alkyl, cycloalkyl, alkenyl, and alkynyl (including groups having at least one unsaturated linkages and from 2 to 8, or 2 to 6 carbon atoms); Ci-6 or C 1 -3 alkoxys; C6-10 aryloxy such as phenoxy; Ci-6 alkylthio; Ci-6 or C1-3 alkylsulfinyl; CI -6 or C1-3 alkylsulfonyl; aminodi(Ci-6 or Ci-3)alkyl; C6-12 aryl having at least one aromatic rings (e.g., phenyl, biphenyl, naphthyl, or the like, each ring either substituted or unsub

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  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de traitement d'alpha-oléfines linéaires qui consiste à : faire passer un courant d'alimentation comprenant des alpha-oléfines linéaires gazeuses à travers un réacteur ; faire passer le courant d'alimentation à travers un liquide dans le réacteur pour produire un courant de réaction, ledit courant de réaction comprenant des alpha-oléfines linéaires, des gouttelettes de polymère, et des gouttelettes d'alpha-oléfines linéaires ; et faire passer le courant de réaction à travers un filtre pour produire un courant de produit gazeux qui sort du réacteur, ledit courant de produit gazeux étant exempt de gouttelettes ayant un diamètre supérieur à 40 micromètres.
PCT/IB2016/057886 2015-12-28 2016-12-21 Procédé de traitement d'alpha-oléfines linéaires WO2017115231A1 (fr)

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US201562271698P 2015-12-28 2015-12-28
US62/271,698 2015-12-28

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023036767A1 (fr) * 2021-09-08 2023-03-16 Sabic Global Technologies B.V. Procédé de rinçage de réacteur

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070137154A1 (en) * 2005-12-16 2007-06-21 Joseph Agnello Vane-type demister
US20090214405A1 (en) * 2005-10-20 2009-08-27 Linde Ag Zentrale Patentabteilung Bubble Column Reactor and Operation Method Thereof
US20130102826A1 (en) * 2011-05-24 2013-04-25 James R. Lattner Systems And Methods For Generating Alpha Olefin Oligomers
EP2689838A1 (fr) * 2012-07-26 2014-01-29 Saudi Basic Industries Corporation Procédé de nettoyage d'un réacteur
WO2015193797A1 (fr) * 2014-06-19 2015-12-23 Sabic Global Technologies B.V. Systèmes de réacteurs améliorés à catalyse homogène

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090214405A1 (en) * 2005-10-20 2009-08-27 Linde Ag Zentrale Patentabteilung Bubble Column Reactor and Operation Method Thereof
US20070137154A1 (en) * 2005-12-16 2007-06-21 Joseph Agnello Vane-type demister
US20130102826A1 (en) * 2011-05-24 2013-04-25 James R. Lattner Systems And Methods For Generating Alpha Olefin Oligomers
EP2689838A1 (fr) * 2012-07-26 2014-01-29 Saudi Basic Industries Corporation Procédé de nettoyage d'un réacteur
WO2015193797A1 (fr) * 2014-06-19 2015-12-23 Sabic Global Technologies B.V. Systèmes de réacteurs améliorés à catalyse homogène

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023036767A1 (fr) * 2021-09-08 2023-03-16 Sabic Global Technologies B.V. Procédé de rinçage de réacteur

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