WO2007016993A1 - Method for preparing linear alpha-olefins - Google Patents

Method for preparing linear alpha-olefins Download PDF

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Publication number
WO2007016993A1
WO2007016993A1 PCT/EP2006/005642 EP2006005642W WO2007016993A1 WO 2007016993 A1 WO2007016993 A1 WO 2007016993A1 EP 2006005642 W EP2006005642 W EP 2006005642W WO 2007016993 A1 WO2007016993 A1 WO 2007016993A1
Authority
WO
WIPO (PCT)
Prior art keywords
ethylene
reactor
feed
olefins
inert gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2006/005642
Other languages
French (fr)
Inventor
Peter Fritz
Heinz BÖLT
Karl-Heinz Hoffmann
Markus Köhler
Hans-Jörg ZANDER
Fuad Mosa
Talal Ali
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Saudi Basic Industries Corp
Original Assignee
Linde GmbH
Saudi Basic Industries Corp
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 Linde GmbH, Saudi Basic Industries Corp filed Critical Linde GmbH
Priority to US11/989,732 priority Critical patent/US20090216057A1/en
Priority to JP2008523147A priority patent/JP2009502818A/en
Publication of WO2007016993A1 publication Critical patent/WO2007016993A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • C07C2/26—Catalytic processes with hydrides or organic compounds
    • C07C2/30—Catalytic processes with hydrides or organic compounds containing metal-to-carbon bond; Metal hydrides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • C07C2531/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
    • C07C2531/04—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing carboxylic acids or their salts
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • C07C2531/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
    • C07C2531/12—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides
    • C07C2531/14—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing organo-metallic compounds or metal hydrides of aluminium or boron

Definitions

  • the present invention relates to a method for preparing linear alpha-olefins by oligomerizing of ethylene in the presence of an organic solvent and a homogenous catalyst.
  • the oligomerization of ethylene using an organometallic catalyst is widely known in the art.
  • the oligomerization is highly exothermic so that reaction heat has to be removed from the reactor to prevent a runaway.
  • DE 43 38 414 Cl discloses a method for the preparation of linear alpha-olefins, wherein polymer grade ethylene is re-circulated to remove the reaction heat. Therefore, ethylene feed (having an ethylene content of approximately 100% with minor amounts of impurities) is introduced into the reactor at a lower temperature, and non-oligomerized monomeric ethylene is removed at a higher temperature, cooled down and re-introduced into the reactor.
  • This object is achieved in that the method is carried out in a reactor being fed with a gaseous feed comprising a minor amount of ethylene and a major amount of an inert gas.
  • the feed comprises at least about 3 wt.% of ethylene.
  • the feed comprises about 5 to about 10 wt.% of ethylene.
  • the inert gas is selected from any of the rare gases, methane, ethane, hydrogen, nitrogen SF 6 , propane, propylene, butane or mixtures thereof, wherein ethane is preferred.
  • the organic solvent may be toluene.
  • the catalyst comprises a zirconium salt of organic acids and at least one or- ganoaluminum compound.
  • the at least one aluminum compound may be Al(C 2 Hs) 3 , Al 2 Cl 3 (C 2 Hs) 3 , AlCl(C 2 Hs) 2 or mixtures thereof.
  • the oligomerization may be carried out in the reactor at a temperature between about 60 to about 10O 0 C.
  • the feed may be introduced into the reactor at a temperature of about 20 to about 50°C.
  • a significant reduction of the ethane/ethylene purge stream from the ethylene cycle (in the amount from t/h to kg/h) is achievable, which may be routed back for reprocessing to an ethylene plant or even has to be considered as a loss.
  • Any purge gas from a polyethylene plant may be utilized as feedstock for the LAO plant utilizing the inventive method.
  • any inert gas which does not liquefy under the oligomerization conditions may be utilized.
  • the preferred inert gas is ethane. Utilizing ethane, the application of low-cost feedstock is possible, since the feedstock can be easily withdrawn upstreams of the high energy- consuming C 2 -splitter of an ethylene plant and may be fed directly into the reactor for oli- gomerizing of ethylene.
  • any other suitable inert gas may be chosen.
  • figure 1 schematically illustrates an inventive method for preparing of linear alpha-olefins by oligomerizing of ethylene.
  • catalyst dissolved in toluene is fed to oligomerization reactor 2 via line 1.
  • a feed comprising ethylene and an inert gas, e.g. ethane, is provided.
  • the feed comprises about 5 to about 10 wt.% of ethylene.
  • the feed is re- circulated through the reactor, two cooling devices, two separators and a compressor and a heater, to remove the reaction heat from the reactor 2.
  • the feed is compressed in the compressor 4, heated in the trim heater 5 to a temperature of about 2O 0 C and is introduced into the oligomerization reactor 2 from the bottom.
  • the oligomerization of ethylene is conducted, when the feed bubbles through the mixture of solvent and catalyst.
  • the products of the oligomerization remain dissolved in the solvent.
  • the temperature in the reactor is about 60-100 0 C.
  • a mixture of ethylene and light alpha-olefins is removed, and, according to the thermodynamic equilibrium, some toluene.
  • the mixture is cooled down in cooling device 7 to a temperature of about 35°C and is collected in separator 8.
  • the liquid obtained, consisting of toluene and alpha-olefins, is re-circulated via line 9 into the separator part of the reactor 2.
  • the part from the separator 8 remaining gaseous is further cooled in cooling device 10 to a temperature of about 5°C and is transferred into the separator 11.
  • the cooling device 10 the cooling is adjusted so that olefins heavier than ethylene are liquefied.
  • the separator may be provided with a recycled C 2 -fraction from a hydrocarbon separation plant (not shown).
  • a mixture of non-consumed ethylene and inert gas may be mixed with a fresh feed thereof, wherein the admixture may be again introduced into the reactor 2 via line 3, compressor 4 and trim heater 5.
  • the liquid products from the separator 11 are transferred via line 14 to an olefin separation (not shown), for example a rectification column.
  • Via line 15 a liquid mixture consisting of toluene, catalyst, dissolved ethylene and linear al- pha-olefins, is removed and may be processed as is well known in the art utilizing a mixing unit 16 and an adsorber 17.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

The present invention relates to a method for preparing linear alpha-olefins by oligomerizing of ethylene in the presence of an organic solvent and a homogenous catalyst, characterized in that the method is carried out in a reactor being fed with a gaseous feed comprising a minor amount of ethylene and a major amount of an inert gas.

Description

METHOD FOR PREPARING LINEAR ALPHA-OLEFINS
The present invention relates to a method for preparing linear alpha-olefins by oligomerizing of ethylene in the presence of an organic solvent and a homogenous catalyst.
The oligomerization of ethylene using an organometallic catalyst is widely known in the art. The oligomerization is highly exothermic so that reaction heat has to be removed from the reactor to prevent a runaway.
DE 43 38 414 Cl discloses a method for the preparation of linear alpha-olefins, wherein polymer grade ethylene is re-circulated to remove the reaction heat. Therefore, ethylene feed (having an ethylene content of approximately 100% with minor amounts of impurities) is introduced into the reactor at a lower temperature, and non-oligomerized monomeric ethylene is removed at a higher temperature, cooled down and re-introduced into the reactor.
It was found that only about 3% of the ethylene feed is used in the oligomerization process, wherein the remainder is utilized as cooling media. Ethylene is quite expensive.
Thus, it is an object of the present invention to provide a method for preparing linear alpha- olefins by oligomerizing of ethylene, which method overcomes the disadvantages of the prior art. Especially, a method shall be provided which may be carried out in a more cost-effective manner.
This object is achieved in that the method is carried out in a reactor being fed with a gaseous feed comprising a minor amount of ethylene and a major amount of an inert gas.
Preferably, the feed comprises at least about 3 wt.% of ethylene.
Most preferably, the feed comprises about 5 to about 10 wt.% of ethylene. In one embodiment, the inert gas is selected from any of the rare gases, methane, ethane, hydrogen, nitrogen SF6, propane, propylene, butane or mixtures thereof, wherein ethane is preferred.
The organic solvent may be toluene.
Preferably, the catalyst comprises a zirconium salt of organic acids and at least one or- ganoaluminum compound.
It is proposed that the zirconium salt has the formula ZrCl4-mXm, wherein X = OCOR or OSO3R' with R and R' being independently alkyl, alkene or phenyl, and wherein O < m < 4.
The at least one aluminum compound may be Al(C2Hs)3, Al2Cl3(C2Hs)3, AlCl(C2Hs)2 or mixtures thereof.
The oligomerization may be carried out in the reactor at a temperature between about 60 to about 10O0C.
Finally, the feed may be introduced into the reactor at a temperature of about 20 to about 50°C.
Surprisingly, it was found that instead of polymer grade ethylene which has been used both so far as starting material and cooling media, this monomer can be substantially replaced by an inert gas only providing the cooling function, but not taking part in the oligomerization process.
Utilizing the inventive method, a significant reduction of the ethane/ethylene purge stream from the ethylene cycle (in the amount from t/h to kg/h) is achievable, which may be routed back for reprocessing to an ethylene plant or even has to be considered as a loss. Any purge gas from a polyethylene plant may be utilized as feedstock for the LAO plant utilizing the inventive method.
Any inert gas which does not liquefy under the oligomerization conditions may be utilized. The preferred inert gas is ethane. Utilizing ethane, the application of low-cost feedstock is possible, since the feedstock can be easily withdrawn upstreams of the high energy- consuming C2-splitter of an ethylene plant and may be fed directly into the reactor for oli- gomerizing of ethylene. However, any other suitable inert gas may be chosen.
It was found that the partly replacement of the conventional 100% ethylene feed by an inert gas does not influence the oligomerization rate and any process conditions.
The invention is now further illustrated with reference to the accompanying drawing wherein figure 1 schematically illustrates an inventive method for preparing of linear alpha-olefins by oligomerizing of ethylene.
In the plant illustrated in figure 1 catalyst dissolved in toluene is fed to oligomerization reactor 2 via line 1. Via line 3 a feed comprising ethylene and an inert gas, e.g. ethane, is provided. Preferably, the feed comprises about 5 to about 10 wt.% of ethylene. The feed is re- circulated through the reactor, two cooling devices, two separators and a compressor and a heater, to remove the reaction heat from the reactor 2. The feed is compressed in the compressor 4, heated in the trim heater 5 to a temperature of about 2O0C and is introduced into the oligomerization reactor 2 from the bottom. In the reactor 2 the oligomerization of ethylene is conducted, when the feed bubbles through the mixture of solvent and catalyst. The products of the oligomerization remain dissolved in the solvent. The temperature in the reactor is about 60-1000C.
Via line 6 a mixture of ethylene and light alpha-olefins is removed, and, according to the thermodynamic equilibrium, some toluene. The mixture is cooled down in cooling device 7 to a temperature of about 35°C and is collected in separator 8. The liquid obtained, consisting of toluene and alpha-olefins, is re-circulated via line 9 into the separator part of the reactor 2. The part from the separator 8 remaining gaseous is further cooled in cooling device 10 to a temperature of about 5°C and is transferred into the separator 11. In the cooling device 10 the cooling is adjusted so that olefins heavier than ethylene are liquefied. Via line 12 the separator may be provided with a recycled C2-fraction from a hydrocarbon separation plant (not shown). Via line 13 a mixture of non-consumed ethylene and inert gas may be mixed with a fresh feed thereof, wherein the admixture may be again introduced into the reactor 2 via line 3, compressor 4 and trim heater 5. The liquid products from the separator 11 are transferred via line 14 to an olefin separation (not shown), for example a rectification column.
Via line 15 a liquid mixture consisting of toluene, catalyst, dissolved ethylene and linear al- pha-olefins, is removed and may be processed as is well known in the art utilizing a mixing unit 16 and an adsorber 17.
The features disclosed in the foregoing description, in the drawing or in the claims may, both separately and in any combination thereof, be material for realizing the invention in diverse forms thereof.

Claims

Claims
1. Method for preparing linear alpha-olefins by oligomerizing of ethylene in the presence of an organic solvent and a homogenous catalyst, characterized in that the method is carried out in a reactor being fed with a gaseous feed comprising a minor amount of ethylene and a major amount of an inert gas.
2. Method according to claim 1, wherein the feed comprises at least about 3 wt.% of ethylene.
3. Method according to claim 2, wherein the feed comprises about 5 to about 10 wt.% of ethylene.
4. Method according to any of the preceding claims, wherein the inert gas is selected from any of the rare gases, methane, ethane, hydrogen, nitrogen SF6, propane, propylene, butane or mixtures thereof, wherein ethane being preferred.
5. Method according to any of the preceding claims, wherein the organic solvent is toluene.
6. Method according to any of the preceding claims, wherein the catalyst comprises a zirconium salt of organic acids and at least one organoaluminum compound.
7. Method according to claim 6, wherein the zirconium salt has the formula ZrCl4-111Xm, wherein X = OCOR or OSO3R' with R and R' being independently alkyl, alkene or phenyl, and wherein 0 < m < 4.
8. Method according to claim 6, wherein the at least one aluminum compound is A1(C2H5)3, Al2Cl3(C2Hs)3, A1C1(C2H5)2 or mixtures thereof.
9. Method according to any of the preceding claims, wherein the oligomerization is carried out in the reactor at a temperature between about 60 to about 100°C.
10. Method according to any of the preceding claims, wherein the feed is introduced into the reactor at a temperature of about 20 to about 5O0C.
PCT/EP2006/005642 2005-07-29 2006-06-13 Method for preparing linear alpha-olefins Ceased WO2007016993A1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US11/989,732 US20090216057A1 (en) 2005-07-29 2006-06-13 Method for Preparing Linear Alpha-Olefins
JP2008523147A JP2009502818A (en) 2005-07-29 2006-06-13 Process for the preparation of linear alpha olefins

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP05016525.7 2005-07-29
EP05016525A EP1748038A1 (en) 2005-07-29 2005-07-29 Method for preparing linear alpha-olefins

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WO2007016993A1 true WO2007016993A1 (en) 2007-02-15

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US (1) US20090216057A1 (en)
EP (1) EP1748038A1 (en)
JP (1) JP2009502818A (en)
CN (1) CN101233093A (en)
MY (1) MY147960A (en)
RU (1) RU2424220C2 (en)
WO (1) WO2007016993A1 (en)
ZA (1) ZA200800890B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011156892A3 (en) * 2010-06-18 2012-02-02 Nova Chemicals (International) S.A. Integrated chemicals complex containing olefins

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102010006589A1 (en) 2010-02-02 2011-08-04 Linde Aktiengesellschaft, 80331 Process for the preparation of linear α-olefins
JP6565525B2 (en) * 2014-09-22 2019-08-28 三菱ケミカル株式会社 Method and apparatus for producing α-olefin low polymer
WO2016047560A1 (en) * 2014-09-22 2016-03-31 三菱化学株式会社 Method for producing α-olefin oligomer
US10513473B2 (en) 2015-09-18 2019-12-24 Chevron Phillips Chemical Company Lp Ethylene oligomerization/trimerization/tetramerization reactor
US10519077B2 (en) 2015-09-18 2019-12-31 Chevron Phillips Chemical Company Lp Ethylene oligomerization/trimerization/tetramerization reactor
US20200087582A1 (en) * 2016-12-19 2020-03-19 Sabic Global Technologies B.V. Method of treating a hydrocarbon stream
FR3105019B1 (en) * 2019-12-18 2022-07-22 Ifp Energies Now GAS/LIQUID OLIGOMERIZATION REACTOR WITH SUCCESSIVE ZONES OF VARIABLE DIAMETER
US11667590B2 (en) 2021-05-26 2023-06-06 Chevron Phillips Chemical Company, Lp Ethylene oligomerization processes

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB879803A (en) * 1959-03-04 1961-10-11 Harold Newby Improvements in the production of alcohols
US3574782A (en) * 1967-10-16 1971-04-13 Exxon Research Engineering Co Process for producing linear alpha olefins
US4486615A (en) * 1960-09-14 1984-12-04 Exxon Research & Engineering Co. Preparation of linear olefin products
DE4338414C1 (en) * 1993-11-10 1995-03-16 Linde Ag Process for the preparation of linear olefins
EP0908436A1 (en) * 1996-04-10 1999-04-14 Kyowa Yuka Co., Ltd. Process for the dimerization of lower olefins
US20040059074A1 (en) * 2000-10-26 2004-03-25 Claudio Bianchini Process for the selective oligomerization of ethylene

Family Cites Families (5)

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US4501885A (en) * 1981-10-14 1985-02-26 Phillips Petroleum Company Diluent and inert gas recovery from a polymerization process
US4855525A (en) * 1987-06-19 1989-08-08 Exxon Chemical Patents Inc. Process for preparing linear alpha-olefins using zirconium adducts as catalysts
FR2669921B1 (en) * 1990-12-04 1995-07-21 Inst Francais Du Petrole PROCESS FOR THE CONVERSION OF ETHYLENE INTO LIGHT ALPHA OLEFINS.
CA2110654C (en) * 1992-12-17 2006-03-21 Albert Rossi Dilute process for the polymerization of ethylene/alpha-olefin copolymer using metallocene catalyst systems
RU2111200C1 (en) * 1995-12-26 1998-05-20 Акционерное общество "Ставропольполимер" Method of preparation of higher $$$-olefins

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB879803A (en) * 1959-03-04 1961-10-11 Harold Newby Improvements in the production of alcohols
US4486615A (en) * 1960-09-14 1984-12-04 Exxon Research & Engineering Co. Preparation of linear olefin products
US3574782A (en) * 1967-10-16 1971-04-13 Exxon Research Engineering Co Process for producing linear alpha olefins
DE4338414C1 (en) * 1993-11-10 1995-03-16 Linde Ag Process for the preparation of linear olefins
EP0908436A1 (en) * 1996-04-10 1999-04-14 Kyowa Yuka Co., Ltd. Process for the dimerization of lower olefins
US20040059074A1 (en) * 2000-10-26 2004-03-25 Claudio Bianchini Process for the selective oligomerization of ethylene

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011156892A3 (en) * 2010-06-18 2012-02-02 Nova Chemicals (International) S.A. Integrated chemicals complex containing olefins

Also Published As

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RU2424220C2 (en) 2011-07-20
CN101233093A (en) 2008-07-30
RU2008107711A (en) 2009-09-10
ZA200800890B (en) 2009-08-26
US20090216057A1 (en) 2009-08-27
EP1748038A1 (en) 2007-01-31
MY147960A (en) 2013-02-15
JP2009502818A (en) 2009-01-29

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