US20040122269A1 - Process for making a linear alpha-olefin oligomer using a heat exchanger - Google Patents
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- B01J31/1805—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms the ligands containing nitrogen
- B01J31/181—Cyclic ligands, including e.g. non-condensed polycyclic ligands, comprising at least one complexing nitrogen atom as ring member, e.g. pyridine
- B01J31/1815—Cyclic ligands, including e.g. non-condensed polycyclic ligands, comprising at least one complexing nitrogen atom as ring member, e.g. pyridine with more than one complexing nitrogen atom, e.g. bipyridyl, 2-aminopyridine
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- 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
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- B01J2208/00017—Controlling the temperature
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- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
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- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
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- B01J2531/02—Compositional aspects of complexes used, e.g. polynuclearity
- B01J2531/0238—Complexes comprising multidentate ligands, i.e. more than 2 ionic or coordinative bonds from the central metal to the ligand, the latter having at least two donor atoms, e.g. N, O, S, P
- B01J2531/0241—Rigid ligands, e.g. extended sp2-carbon frameworks or geminal di- or trisubstitution
- B01J2531/0244—Pincer-type complexes, i.e. consisting of a tridentate skeleton bound to a metal, e.g. by one to three metal-carbon sigma-bonds
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- C07C2531/22—Organic complexes
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- C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F110/02—Ethene
Definitions
- the invention pertains to a process for making a linear alpha-olefin oligomer from ethylene in a reactor having a liquid and a gas phase, in the presence of a catalyst.
- Alpha-olefin oligomers are compounds or a mixture of compounds with the general formula H 2 C ⁇ CH—(CH 2 CH 2 ) n H wherein n is an integer of 1 or greater. In such oligomers the alpha-olefin oligomer is usually a mixture of alpha-olefin oligomers with a mean number n from 1 to 20, preferably from 2 to 10.
- Alpha-olefin oligomers prepared according to the process of the present invention preferably have an average molecular weight between about 50 and about 350, more preferably between about 60 and about 280, even more preferably between about 80 and about 210.
- the reaction of ethylene in the presence of the above iron complex is usually run in the liquid phase in a well-mixed reactor, typically using an aprotic organic solvent. This reaction generates a large amount of heat, which should be removed.
- aprotic organic solvent typically used to remove heat from the reactor system.
- the process temperature which usually is between about 35° C. and about 90° C., more preferably between about 35° C. and about 75° C., affects the cost of manufacture of the alpha-olefins in several ways. The higher the temperature the smaller the heat exchangers which have to be applied to the reactor(s), which generally lowers cost.
- the decay of the active oligomerization catalyst increases with increasing temperature. It is found that maximum volumetric production of alpha-olefins coupled with good absolute productivity of the catalyst usually occurs in the range of about 45° C. to about 75° C., so this temperature range is preferred. Finally, the temperature also affects the bubble point pressure, the amount of ethylene in the liquid phase, and the catalyst selectivity. The higher the temperature the higher the pressure needed to maintain catalyst selectivity, which increases capital cost of the manufacturing plant because of, for example, the need for thicker vessels and larger compressors to attain higher ethylene pressures. Higher pressure also increases energy costs.
- the amount of ethylene (ethene) oligomerization catalyst used in the reaction will preferably be the maximum permitted by the cooling capacity of the reactor(s) and the ethylene mass transfer from the gas to the liquid phase. Catalyst may be added to the first reactor only or to one or more subsequent reactors in series. Differing amounts of catalyst may be added to each reactor.
- the oligomerization is quite exothermic, about 100 kJ/mole of ethylene oligomerized, and as such cooling will usually be applied to the reactor(s) to maintain the desired process temperature while maintaining high volumetric productivity of the reactor(s).
- cooling is accomplished by running cooling tubes through the liquid in the interior of one or more of the reactors to cool the contents.
- Another method of cooling is to have one or more heat exchangers external to the reactors and connected to the reactors by a liquid loop to cool the reactor contents. These external heat exchangers may be typical shell and tube exchangers.
- the reactors may also be jacketed with a cooling jacket. Some or all of the feeds to some or all of the reactors may be cooled to allow the sensible heat of the ingredients to cool the reactors. All these liquid cooling methods, however, suffer from the disadvantage of wax and polyethylene fouling of the coolers, which necessitates regular shut down of the reactor to allow cleaning of the coolers. Furthermore, wax and polyethylene fouling may increase the paraffinicity of the solvent.
- linear alpha-olefin oligomers can be made in a reactor comprising a liquid and a gas phase, comprising the steps of catalytically oligomerizing ethylene in the presence of an iron complex of a 2,6-bis(arylimino)pyridine derivative, to an alpha-olefin oligomer with an average molecular weight between about 50 and about 350 under release of heat, and removing the heat with a heat exchanger, which is not in direct contact with the liquid phase, using at least part of the gas phase as a coolant medium.
- This method provides a cooling system having its cooling elements outside the liquid reaction medium. Since wax and polyethylene have high boiling points, deposit of wax and polyethylene can no longer occur, and fouling of the heat exchanger is effectively prevented.
- FIG. 1 is a scheme of an apparatus for performing the method according to the invention with the heat exchanger positioned outside the reactor.
- FIG. 2 is a scheme of an apparatus for performing the method according to the invention with the heat exchanger positioned inside the reactor.
- the heat exchanger according to this invention is a conventional type, such as a shell- and tube-type, and the like.
- the heat exchanger is internally cooled with conventional cooling fluids, like water, ammonia, Freon® coolant, and the like.
- the reaction heat causes the solvents, reactants, and/or reaction products, which are present in the reaction medium, to evaporate and subsequently to be cooled by the heat exchanger, after which it works as a coolant medium for the reactor.
- the heat exchanger can be placed inside or outside the reactor. When the heat exchanger is placed inside the reactor it is preferred that some condensation occurs on the heat exchanger surface.
- the heat exchanger When the heat exchanger is placed outside the reactor, it is preferred to apply a forced circulation of the reactor coolant medium from the gas phase of the reactor through heat exchanger(s), compressor(s)/pump(s) and optionally a gas-liquid separator back to the liquid phase of the reactor. Additionally, this will improve the mixing in the reactor. After cooling the reactor coolant medium in this loop, some condensation can occur. This allows application of a separate gas and liquid return to the reactor using a gas-liquid separator. Furthermore, it is possible to deliberately remove (part of) this liquid phase from this gas-liquid separator and route this directly to the product work-up section. Finally, if full condensation occurs, return of this liquid to the reactor can be achieved by a pump instead of a compressor, which lowers costs.
- This reactor coolant medium is selected from an alkane, alkene, and aromatic compound, and mixtures thereof, preferably propane, n-pentane, isopentane, ethylene, 1-butene, o-, m-, and p-xylene, and toluene, and mixtures thereof.
- An additional advantage of the present process is the possibility to apply only one reactor, because the efficiency and the lack of fouling no longer necessitates the use of a plurality of small reactors. This adds considerably to the lowering of costs of the oligomerization process.
- iron complexes of the 2,6-bis(arylimino)pyridine type that can be used in the above process are known in the art, and are described in WO 02/00339, WO 02/12151, WO 02/06192, WO 02/28805, WO 01/58874, and WO 99/02472. Any of these complexes can be used.
- R1 is H or CH 3 ;
- R2 is H, tert-butyl or phenyl
- R3 is H, tert-butyl or OR′ wherein R′ stands for CH 3 ,
- aryl means an aromatic group, such as phenyl, naphthyl, thienyl, pyridyl, pyrrolyl, and the like. Phenyl is the preferred aryl group. Preferred phenyl groups are substituted with CH 3 , tert-butyl, F, or OR′ wherein R′ stands for CH 3 or Si(CH 3 ) 3 .
- an aluminum-based co-catalyst preferably a methylaluminoxane
- a co-catalyst such as an alkylaluminum compound
- an iron complex of a 2,6-bis(arylimino)pyridine derivative such as a complex of the 2,6-bis(arylimino)pyridine derivative with FeCl 2
- an alkylaluminum compound preferably an aluminoxane
- alkylaluminum compounds include methylaluminoxane (which is an oligomer with the general formula (MeAlO) n ), (C 2 H 5 ) 2 AlC 1 , C 2 H 5 AlCl 2 , (C 2 H 5 ) 3 Al and ((CH 3 ) 2 CHCH 2 ) 3 Al.
- a particularly preferred aluminoxane is methyl aluminoxane.
- the ratio of aluminum (as alkylaluminum compound) to iron (as a complex) in the oligomerization may be about 10 to about 10,000.
- Another preferred component of the catalyst systems herein is a second co-catalyst compound selected from formula ZnR′ 2 wherein each R′, which may be the same or different, is selected from hydrogen, optionally substituted C 1 -C 20 hydrocarbyl, phenyl, F, Cl, Br, I, SR′′, NR′′ 2 , OH, OR′′, CN, NC wherein R′′, which within the same molecule may be the same or different, is C 1 -C 20 hydrocarbyl.
- the second co-catalyst compound is ZnR′ 2 wherein R′ is C 1 -C 20 hydrocarbyl, more preferably C 1 -C 20 alkyl, even more preferably C 1 -C 6 alkyl.
- Suitable alkyl groups include methyl, ethyl, propyl, butyl, and the like. It is especially preferred that the R′ group is a C 1 -C 3 alkyl, especially ethyl.
- the second co-catalyst is particularly valuable in combination with the aluminium-based co-catalyst for increasing the selectivity of linear alpha olefins in ethylene oligomerization reactions, and decreasing the amount of unwanted by-products such as branched olefins, internal olefins, 2,2-disubstituted olefins, and dienes.
- the active catalyst system may be formed by mixing together the iron complex of a 2,6-bis(arylimino)pyridine derivative or a mixture of the iron acetylacetonate complex and the appropriate 2,6-bis(arylimino)pyridine derivative (ligand), first co-catalyst compound, second co-catalyst compound and any optional additional compounds, preferably in a solvent.
- reactor coolant medium An important item in the capital cost of this manufacturing plant and in its cost of operation is the amount of reactor coolant medium that must be recycled in the process. Recycling of a gaseous reactor coolant medium often involves recompression to feed one or more of the reactors. Compressors and associated equipment add greatly to capital and operational costs.
- the coolant medium is preferably selected to completely dissolve ethylene. In this case the coolant medium only requires a single reactor and a condenser, whereas a simple recycle pump is sufficient. Thus expensive recycling, such as the use of an expensive recycle blower, is no longer required, which adds further to the advantages of the present method.
- FIG. 1 shows a reactor 2 with a liquid phase 3 and a gas phase 4 being in equilibrium through gas/liquid interface 12 .
- the liquid phase comprises ethylene, the nickel, palladium, cobalt, titanium, zirconium, hafnium, vanadium, chromium, molybdenum, or tungsten complex of a 2,6-bis(arylimino)pyridine derivative, alpha-olefin oligomer, and optionally solvents and auxiliaries such as a co-catalyst.
- the optional solvents are selected as to dissolve ethylene.
- the reactor 2 contains an inlet 10 through which the reactor feed 1 (usually ethylene) is introduced into the reactor 2 , a gas outlet 11 , and a reactor bottom outlet 9 .
- outlet is connected through a conduit 14 to heat exchanger 5 a , which is connected through conduit 15 to gas-liquid separator 6 .
- conduit 15 may contain a compressor 7 a .
- Gas-liquid separator 6 has an outlet for transporting the liquid, optionally through a pump 8 , to obtain a pressurized liquid stream 17 that is recycled via conduit 19 to reactor 2 .
- the gas leaves the gas-liquid separator 6 through conduit 16 , which may optionally comprise compressor 7 b and/or heat exchanger 5 b , to obtain a cooled gas stream 18 that is recycled to reactor 2 .
- conduit 15 can directly be connected to compressor 7 b and/or heat exchanger 5 b , if present, or to conduit 19 .
- Reactor 2 may contain an optional entrainment separator 13 .
- FIG. 2 shows another embodiment of the invention.
- the reactor feed 1 is introduced into the reactor 2 through inlet 10 .
- the liquid phase 3 in the reactor is in equilibrium with the gas phase 4 through gas/liquid interface 12 .
- a heat exchanger 20 is placed, which is not in contact with the liquid phase 3 .
- the section of the gas phase 4 may optionally contain an entrainment separator 13 .
- the heat exchanger 20 cools the gas, after which at least part of the gas condenses and the cooled condensate falls down from the surface of the heat exchanger 20 into the liquid phase 3 , thereby cooling the liquid medium.
- the reaction product may then be discharged from the reactor through the reactor bottom outlet 9 .
- an apparatus for performing the process of making linear alpha-olefin oligomer described above comprising a reactor, which can accommodate a liquid and a gas phase, an inlet through which the reactor feed can be introduced into the reactor, a reactor bottom outlet to remove the oligomer, and a heat exchanger, which is positioned in the gas phase to condense the gas and allow the condensate to fall therefrom to cool the liquid phase, and optionally, an entrainment separator, and/or a gas-liquid separator.
Abstract
The invention pertains to a process for making a linear alpha-olefin oligomer in a reactor comprising a liquid and a gas phase, comprising the steps of catalytically oligomerizing ethylene in the presence of an iron complex of a 2,6-bis(arylimino)pyridine derivative, to an alpha-olefin oligomer under release of heat, and removing the heat with a heat exchanger, which is not in direct contact with the liquid phase, using at least part of the gas phase as a coolant medium. The invention further relates to an apparatus to perform said process.
Description
- The invention pertains to a process for making a linear alpha-olefin oligomer from ethylene in a reactor having a liquid and a gas phase, in the presence of a catalyst.
- Various processes are known for the production of higher linear alpha olefins (See, for example, D. Vogt, Oligomerisation of ethylene to higher a-olefins in Applied Homogeneous Catalysis with Organometallic Compounds, Ed. B. Cornils, W. A. Herrmann, 2nd Edition, Vol. 1, Ch. 2.3.1.3, page 240-253, Wiley-VCH 2002). These commercial processes afford either a Poisson or Schulz-Flory oligomer product distribution. In such a process, a wide range of oligomers is typically made.
- In WO 02/00339, WO 02/12151, WO 02/06192, WO 02/28805, WO 01/58874, and WO 99/02472 novel Fe-based ethylene oligomerization catalysts are described that show high activity and high selectivity towards linear alpha-olefins. These catalysts, which are incorporated by reference, are based on iron complexes of a selected 2,6-pyridinedicarboxaldehyde bisimine or a selected 2,6-diacylpyridine bisimine.
- In the present invention the term “bis-(arylimino)-pyridine” is used to describe both classes of ligands. Alpha-olefin oligomers are compounds or a mixture of compounds with the general formula H2C═CH—(CH2CH2)nH wherein n is an integer of 1 or greater. In such oligomers the alpha-olefin oligomer is usually a mixture of alpha-olefin oligomers with a mean number n from 1 to 20, preferably from 2 to 10. Alpha-olefin oligomers prepared according to the process of the present invention preferably have an average molecular weight between about 50 and about 350, more preferably between about 60 and about 280, even more preferably between about 80 and about 210.
- The reaction of ethylene in the presence of the above iron complex is usually run in the liquid phase in a well-mixed reactor, typically using an aprotic organic solvent. This reaction generates a large amount of heat, which should be removed. As described in WO 02/06192 it is preferred to install a plurality of small reactors in combination with several heat exchangers to help provide sufficient cooling capacity for the reactor system. The process temperature, which usually is between about 35° C. and about 90° C., more preferably between about 35° C. and about 75° C., affects the cost of manufacture of the alpha-olefins in several ways. The higher the temperature the smaller the heat exchangers which have to be applied to the reactor(s), which generally lowers cost. The decay of the active oligomerization catalyst increases with increasing temperature. It is found that maximum volumetric production of alpha-olefins coupled with good absolute productivity of the catalyst usually occurs in the range of about 45° C. to about 75° C., so this temperature range is preferred. Finally, the temperature also affects the bubble point pressure, the amount of ethylene in the liquid phase, and the catalyst selectivity. The higher the temperature the higher the pressure needed to maintain catalyst selectivity, which increases capital cost of the manufacturing plant because of, for example, the need for thicker vessels and larger compressors to attain higher ethylene pressures. Higher pressure also increases energy costs.
- The amount of ethylene (ethene) oligomerization catalyst used in the reaction will preferably be the maximum permitted by the cooling capacity of the reactor(s) and the ethylene mass transfer from the gas to the liquid phase. Catalyst may be added to the first reactor only or to one or more subsequent reactors in series. Differing amounts of catalyst may be added to each reactor. The oligomerization is quite exothermic, about 100 kJ/mole of ethylene oligomerized, and as such cooling will usually be applied to the reactor(s) to maintain the desired process temperature while maintaining high volumetric productivity of the reactor(s).
- In the prior art cooling is accomplished by running cooling tubes through the liquid in the interior of one or more of the reactors to cool the contents. Another method of cooling is to have one or more heat exchangers external to the reactors and connected to the reactors by a liquid loop to cool the reactor contents. These external heat exchangers may be typical shell and tube exchangers. The reactors may also be jacketed with a cooling jacket. Some or all of the feeds to some or all of the reactors may be cooled to allow the sensible heat of the ingredients to cool the reactors. All these liquid cooling methods, however, suffer from the disadvantage of wax and polyethylene fouling of the coolers, which necessitates regular shut down of the reactor to allow cleaning of the coolers. Furthermore, wax and polyethylene fouling may increase the paraffinicity of the solvent.
- It would be advantageous to devise a process without the above disadvantages. It has now been found that linear alpha-olefin oligomers can be made in a reactor comprising a liquid and a gas phase, comprising the steps of catalytically oligomerizing ethylene in the presence of an iron complex of a 2,6-bis(arylimino)pyridine derivative, to an alpha-olefin oligomer with an average molecular weight between about 50 and about 350 under release of heat, and removing the heat with a heat exchanger, which is not in direct contact with the liquid phase, using at least part of the gas phase as a coolant medium.
- This method provides a cooling system having its cooling elements outside the liquid reaction medium. Since wax and polyethylene have high boiling points, deposit of wax and polyethylene can no longer occur, and fouling of the heat exchanger is effectively prevented.
- The invention is illustrated by the following Figures, which are not meant to limit the invention in any way, showing a scheme of an apparatus that can be used for performing the process of the invention.
- FIG. 1 is a scheme of an apparatus for performing the method according to the invention with the heat exchanger positioned outside the reactor.
- FIG. 2 is a scheme of an apparatus for performing the method according to the invention with the heat exchanger positioned inside the reactor.
- The heat exchanger according to this invention is a conventional type, such as a shell- and tube-type, and the like. The heat exchanger is internally cooled with conventional cooling fluids, like water, ammonia, Freon® coolant, and the like. The reaction heat causes the solvents, reactants, and/or reaction products, which are present in the reaction medium, to evaporate and subsequently to be cooled by the heat exchanger, after which it works as a coolant medium for the reactor. The heat exchanger can be placed inside or outside the reactor. When the heat exchanger is placed inside the reactor it is preferred that some condensation occurs on the heat exchanger surface. When the heat exchanger is placed outside the reactor, it is preferred to apply a forced circulation of the reactor coolant medium from the gas phase of the reactor through heat exchanger(s), compressor(s)/pump(s) and optionally a gas-liquid separator back to the liquid phase of the reactor. Additionally, this will improve the mixing in the reactor. After cooling the reactor coolant medium in this loop, some condensation can occur. This allows application of a separate gas and liquid return to the reactor using a gas-liquid separator. Furthermore, it is possible to deliberately remove (part of) this liquid phase from this gas-liquid separator and route this directly to the product work-up section. Finally, if full condensation occurs, return of this liquid to the reactor can be achieved by a pump instead of a compressor, which lowers costs. This reactor coolant medium is selected from an alkane, alkene, and aromatic compound, and mixtures thereof, preferably propane, n-pentane, isopentane, ethylene, 1-butene, o-, m-, and p-xylene, and toluene, and mixtures thereof.
- An additional advantage of the present process is the possibility to apply only one reactor, because the efficiency and the lack of fouling no longer necessitates the use of a plurality of small reactors. This adds considerably to the lowering of costs of the oligomerization process.
- The iron complexes of the 2,6-bis(arylimino)pyridine type that can be used in the above process are known in the art, and are described in WO 02/00339, WO 02/12151, WO 02/06192, WO 02/28805, WO 01/58874, and WO 99/02472. Any of these complexes can be used. Best results, however, are obtained with such iron complexes wherein one of the aryl moieties of the 2,6-bis(arylimino)pyridine derivative is 2,6-disubstituted with the group CH2R or C2H5R, wherein R is selected from H, F, and substituted or unsubstituted aryl, preferably selected from H and F, and the other aryl moiety is 2,6-unsubstituted, or wherein both aryl moieties of the 2,6-bis(arylimino)pyridine derivative are 2,6-disubstituted with F or Cl.
-
- wherein
- R1 is H or CH3;
- R2 is H, tert-butyl or phenyl; and
- R3 is H, tert-butyl or OR′ wherein R′ stands for CH3,
-
- The term “aryl” means an aromatic group, such as phenyl, naphthyl, thienyl, pyridyl, pyrrolyl, and the like. Phenyl is the preferred aryl group. Preferred phenyl groups are substituted with CH3, tert-butyl, F, or OR′ wherein R′ stands for CH3 or Si(CH3)3.
- In a preferred embodiment an aluminum-based co-catalyst, preferably a methylaluminoxane, is added to the liquid phase. Where a co-catalyst such as an alkylaluminum compound is required or preferred for the active catalyst species, an iron complex of a 2,6-bis(arylimino)pyridine derivative, such as a complex of the 2,6-bis(arylimino)pyridine derivative with FeCl2, may be reacted with an alkylaluminum compound, preferably an aluminoxane, to form an active ethylene oligomerization species. Specific alkylaluminum compounds include methylaluminoxane (which is an oligomer with the general formula (MeAlO)n), (C2H5)2AlC1, C2H5AlCl2, (C2H5)3Al and ((CH3)2CHCH2)3Al. A particularly preferred aluminoxane is methyl aluminoxane. The ratio of aluminum (as alkylaluminum compound) to iron (as a complex) in the oligomerization may be about 10 to about 10,000.
- Another preferred component of the catalyst systems herein is a second co-catalyst compound selected from formula ZnR′2 wherein each R′, which may be the same or different, is selected from hydrogen, optionally substituted C1-C20 hydrocarbyl, phenyl, F, Cl, Br, I, SR″, NR″2, OH, OR″, CN, NC wherein R″, which within the same molecule may be the same or different, is C1-C20 hydrocarbyl.
- In preferred catalyst systems herein, the second co-catalyst compound is ZnR′2 wherein R′ is C1-C20 hydrocarbyl, more preferably C1-C20 alkyl, even more preferably C1-C6 alkyl. Suitable alkyl groups include methyl, ethyl, propyl, butyl, and the like. It is especially preferred that the R′ group is a C1-C3 alkyl, especially ethyl.
- The second co-catalyst is particularly valuable in combination with the aluminium-based co-catalyst for increasing the selectivity of linear alpha olefins in ethylene oligomerization reactions, and decreasing the amount of unwanted by-products such as branched olefins, internal olefins, 2,2-disubstituted olefins, and dienes.
- It has been noted that particularly high selectivity of linear alpha olefins is achieved when the molar ratio of the metal of the aluminium-based co-catalyst to the metal of the second co-catalyst is in the range of from about 5:1 to about 1:5, preferably from about 3:1 to about 1:3, more preferably from about 2:1 to about 1:2 and especially about 1:1.
- It is possible to add further optional components to the catalyst systems herein, for example, Lewis acids and bases such as those disclosed in WO02/28805.
- The active catalyst system may be formed by mixing together the iron complex of a 2,6-bis(arylimino)pyridine derivative or a mixture of the iron acetylacetonate complex and the appropriate 2,6-bis(arylimino)pyridine derivative (ligand), first co-catalyst compound, second co-catalyst compound and any optional additional compounds, preferably in a solvent.
- An important item in the capital cost of this manufacturing plant and in its cost of operation is the amount of reactor coolant medium that must be recycled in the process. Recycling of a gaseous reactor coolant medium often involves recompression to feed one or more of the reactors. Compressors and associated equipment add greatly to capital and operational costs. In the present method the coolant medium is preferably selected to completely dissolve ethylene. In this case the coolant medium only requires a single reactor and a condenser, whereas a simple recycle pump is sufficient. Thus expensive recycling, such as the use of an expensive recycle blower, is no longer required, which adds further to the advantages of the present method.
- FIG. 1 shows a
reactor 2 with aliquid phase 3 and agas phase 4 being in equilibrium through gas/liquid interface 12. The liquid phase comprises ethylene, the nickel, palladium, cobalt, titanium, zirconium, hafnium, vanadium, chromium, molybdenum, or tungsten complex of a 2,6-bis(arylimino)pyridine derivative, alpha-olefin oligomer, and optionally solvents and auxiliaries such as a co-catalyst. The optional solvents are selected as to dissolve ethylene. Thereactor 2 contains aninlet 10 through which the reactor feed 1 (usually ethylene) is introduced into thereactor 2, agas outlet 11, and areactor bottom outlet 9. In the embodiment of FIG. 1, outlet is connected through aconduit 14 toheat exchanger 5 a, which is connected throughconduit 15 to gas-liquid separator 6. If necessary,conduit 15 may contain acompressor 7 a. Gas-liquid separator 6 has an outlet for transporting the liquid, optionally through apump 8, to obtain a pressurizedliquid stream 17 that is recycled viaconduit 19 toreactor 2. The gas leaves the gas-liquid separator 6 throughconduit 16, which may optionally comprisecompressor 7 b and/orheat exchanger 5 b, to obtain a cooledgas stream 18 that is recycled toreactor 2. If no condensation occurs inconduit 15, gas-liquid separator 6, and pump 8 are redundant and may be deleted. In thatcase conduit 15 can directly be connected tocompressor 7 b and/orheat exchanger 5 b, if present, or toconduit 19.Reactor 2 may contain anoptional entrainment separator 13. - FIG. 2 shows another embodiment of the invention. In this embodiment the
reactor feed 1 is introduced into thereactor 2 throughinlet 10. Theliquid phase 3 in the reactor is in equilibrium with thegas phase 4 through gas/liquid interface 12. In the section of the reactor containing thegas phase 4, aheat exchanger 20 is placed, which is not in contact with theliquid phase 3. The section of thegas phase 4 may optionally contain anentrainment separator 13. Theheat exchanger 20 cools the gas, after which at least part of the gas condenses and the cooled condensate falls down from the surface of theheat exchanger 20 into theliquid phase 3, thereby cooling the liquid medium. The reaction product may then be discharged from the reactor through thereactor bottom outlet 9. - Hence, according to a further aspect of the present invention there is provided an apparatus for performing the process of making linear alpha-olefin oligomer described above, comprising a reactor, which can accommodate a liquid and a gas phase, an inlet through which the reactor feed can be introduced into the reactor, a reactor bottom outlet to remove the oligomer, and a heat exchanger, which is positioned in the gas phase to condense the gas and allow the condensate to fall therefrom to cool the liquid phase, and optionally, an entrainment separator, and/or a gas-liquid separator.
Claims (25)
1. A process for making a linear alpha-olefin oligomer in a reactor comprising a liquid and a gas phase, comprising the steps of catalytically oligomerizing ethylene in the presence of an iron complex of a 2,6-bis(arylimino)pyridine derivative, to an alpha-olefin oligomer under release of heat, and removing the heat with a heat exchanger which is not in direct contact with the liquid phase, using at least part of the gas phase as a coolant medium.
2. The process of claim 1 wherein an aluminum-based co-catalyst is added to the liquid phase.
3. The process of claim 2 wherein the aluminum-based co-catalyst is an aluminoxane selected from the group consisting of methyl aluminoxane, alkyl-modified methyl aluminoxane, and mixtures thereof.
4. The process of claim 3 wherein the aluminum-based co-catalyst is a methyl aluminoxane.
5. The process of claim 1 wherein the oligomer is an alpha-olefin oligomer with an average molecular weight between about 50 and about 350.
6. The process of claim 5 wherein the average molecular weight is between about 60 and about 280.
7. The process of claim 6 wherein the average molecular weight is between about 80 and about 210.
8. The process of claim 2 to which is added a second co-catalyst compound which comprises one or more compounds of the formula ZnR′2 wherein each R′, which may be the same or different, is selected from hydrogen, optionally substituted C1-C20 hydrocarbyl, phenyl, F, Cl, Br, I, SR″, NR″2, OH, OR″, CN, NC wherein R″, which within the same molecule may the same or different, is C1-C20 hydrocarbyl.
9. The process of claim 8 wherein R′ is C1-C20 hydrocarbyl.
10. The process of claim 9 wherein R′ is C1-C20 alkyl.
11. The process of claim 10 wherein R′ is C1-C6 alkyl.
12. The process of claim 11 wherein R′ is ethyl.
13. The process of claim 1 wherein one of the aryl moieties of the 2,6-bis(arylimino)pyridine derivative is 2,6-disubstituted with the group CH2R or C2H5R, wherein R is selected from H and F, and the other aryl moiety is 2,6-unsubstituted, or wherein both aryl moieties of the 2,6-bis(arylimino)pyridine derivative are 2,6-disubstituted with F or Cl.
15. The process of claim 1 wherein the coolant medium is selected from the group consisting of an alkane, an alkene, and an aromatic compound, and mixtures thereof.
16. The process of claim 1 wherein the coolant medium is selected from the group consisting of propane, n-pentane, isopentane, ethylene, 1-butene, o-, m-, and p-xylene, and toluene, and mixtures thereof.
17. An apparatus for performing the process of making linear alpha-olefin oligomer of claim 1 comprising a reactor which can accommodate a liquid phase and a gas phase, an inlet through which the reactor feed is introduced into the reactor, a reactor bottom outlet through which the oligomer is removed, a heat exchanger which is positioned in the gas phase to condense the gas and allow the condensate to fall therefrom to cool the liquid phase thereby cooling the liquid, and optionally, a gas outlet and/or an entrainment separator.
18. The apparatus of claim 17 wherein a gas entrainment separator which is positioned in the gas phase.
19. An apparatus for performing the process of making linear alpha-olefin oligomer of claim 1 comprising 1) a reactor which can accommodate a liquid phase and a gas phase, a reactor feed inlet, a gas outlet, and a reactor bottom outlet for the reaction products, 2) a heat exchanger which is positioned outside of the reactor, receives gas from the reactor gas outlet, and cools the gas, wherein said gas flows from the heat exchanger through a first gas conduit where part of the gas condenses, 3) a gas-liquid separator which has a gas outlet and a liquid outlet, receives gas and liquid from the heat exchanger, and separates gas, which exits the separator through a second gas conduit and is recycled to the reactor, from liquid, which exits the separator through a liquid conduit and is recycled to the reactor.
20. The apparatus of claim 19 further comprising a compressor between the heat exchanger and the gas-liquid separator.
21. The apparatus of claim 20 further comprising a pump in the liquid conduit.
22. The apparatus of claim 20 further comprising a compressor and/or a heat exchanger in the second gas conduit.
23. The apparatus of claim 20 further comprising an entrainment separator in the reactor in the gas phase.
24. An apparatus for performing the process of making linear alpha-olefin oligomer of claim 1 comprising 1) a reactor which can accommodate a liquid phase and a gas phase, a reactor feed inlet, a gas outlet, and a reactor bottom outlet for the reaction products, and 2) a heat exchanger which is positioned outside of the reactor, receives gas from the reactor gas outlet, and cools the gas, wherein said gas flows from the heat exchanger through a gas conduit and is recycled to the reactor.
25. The apparatus of claim 15 further comprising a compressor and/or a heat exchanger in the gas conduit.
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Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20040122271A1 (en) * | 2002-09-25 | 2004-06-24 | Van Zon Arie | Process for making a linear alpha-olefin oligomer using a heat exchanger |
US20070112150A1 (en) * | 2005-07-21 | 2007-05-17 | Small Brooke L | Diimine metal complexes, methods of synthesis, and method of using in oligomerization and polymerization |
US20080004441A1 (en) * | 2005-07-21 | 2008-01-03 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US20080004459A1 (en) * | 2005-07-21 | 2008-01-03 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US7820581B2 (en) | 2004-02-20 | 2010-10-26 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US7902415B2 (en) | 2007-12-21 | 2011-03-08 | Chevron Phillips Chemical Company Lp | Processes for dimerizing or isomerizing olefins |
US7910670B2 (en) | 2005-08-19 | 2011-03-22 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US7994376B2 (en) | 2004-02-19 | 2011-08-09 | Chevron Phillips Chemical Company Lp | Olefin oligomerization |
US8329608B2 (en) | 2004-02-20 | 2012-12-11 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US9550841B2 (en) | 2004-02-20 | 2017-01-24 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US9586872B2 (en) | 2011-12-30 | 2017-03-07 | Chevron Phillips Chemical Company Lp | Olefin oligomerization methods |
US9944661B2 (en) | 2016-08-09 | 2018-04-17 | Chevron Phillips Chemical Company Lp | Olefin hydroboration |
US10214463B2 (en) | 2014-09-22 | 2019-02-26 | Mitsubishi Chemical Corporation | Production method and production apparatus of α-olefin oligomer |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7081506B2 (en) * | 2003-10-23 | 2006-07-25 | Fina Technology, Inc. | Ethylene polymerization employing bis-imino pyridinyl transition metal catalyst components |
US7129304B1 (en) | 2005-07-21 | 2006-10-31 | Chevron Phillips Chemical Company Lp | Dimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
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Citations (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2978441A (en) * | 1957-05-23 | 1961-04-04 | Phillips Petroleum Co | Polyolefin reactor control |
US3461109A (en) * | 1964-11-09 | 1969-08-12 | Phillips Petroleum Co | Process for the polymerization of conjugated dienes |
US3565873A (en) * | 1967-09-25 | 1971-02-23 | Copolymer Rubber & Chem Corp | Method and apparatus for polymerizing monomeric materials |
US3968090A (en) * | 1973-12-28 | 1976-07-06 | Mitsubishi Rayon Co., Ltd. | Method for removing heat of polymerization |
US4709111A (en) * | 1987-02-27 | 1987-11-24 | Uop Inc. | Oligomerization process with integrated heat utilization |
US5198563A (en) * | 1989-08-10 | 1993-03-30 | Phillips Petroleum Company | Chromium compounds and uses thereof |
US5382738A (en) * | 1991-12-13 | 1995-01-17 | Phillips Petroleum Company | Chromium compounds and uses in trimerization or oligomerization |
US5541270A (en) * | 1993-05-20 | 1996-07-30 | Bp Chemicals Limited | Polymerization process |
US5550305A (en) * | 1991-10-16 | 1996-08-27 | Amoco Corporation | Ethylene trimerization |
US20040116758A1 (en) * | 2002-09-25 | 2004-06-17 | De Boer Eric Johannes Maria | Catalyst systems for ethylene oligomerisation to linear alpha olefins |
US20040122271A1 (en) * | 2002-09-25 | 2004-06-24 | Van Zon Arie | Process for making a linear alpha-olefin oligomer using a heat exchanger |
US6825297B1 (en) * | 1999-05-14 | 2004-11-30 | The Dow Chemical Company | Transition metal complexes and olefin polymerization process |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB9819847D0 (en) * | 1998-09-12 | 1998-11-04 | Bp Chem Int Ltd | Novel compounds |
GC0000291A (en) * | 2000-06-30 | 2006-11-01 | Shell Int Research | Ligands and catalyst systems thereof for ethylene oligomerisation to linear alpha olefins |
US6534691B2 (en) * | 2000-07-18 | 2003-03-18 | E. I. Du Pont De Nemours And Company | Manufacturing process for α-olefins |
-
2003
- 2003-09-23 CN CNB038229943A patent/CN100519491C/en not_active Expired - Fee Related
- 2003-09-23 RU RU2005112253/04A patent/RU2312848C2/en not_active IP Right Cessation
- 2003-09-23 US US10/668,933 patent/US20040122269A1/en not_active Abandoned
- 2003-09-23 WO PCT/EP2003/010709 patent/WO2004029012A1/en active Application Filing
- 2003-09-23 ES ES03753462T patent/ES2324030T3/en not_active Expired - Lifetime
- 2003-09-23 AU AU2003271645A patent/AU2003271645A1/en not_active Abandoned
- 2003-09-23 DE DE60327784T patent/DE60327784D1/en not_active Expired - Lifetime
- 2003-09-23 AT AT03753462T patent/ATE432248T1/en not_active IP Right Cessation
- 2003-09-23 EP EP03753462A patent/EP1546069B1/en not_active Revoked
- 2003-09-23 JP JP2004539030A patent/JP4498926B2/en not_active Expired - Fee Related
- 2003-09-23 CA CA2499887A patent/CA2499887C/en not_active Expired - Fee Related
-
2005
- 2005-03-11 ZA ZA2005/02082A patent/ZA200502082B/en unknown
Patent Citations (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2978441A (en) * | 1957-05-23 | 1961-04-04 | Phillips Petroleum Co | Polyolefin reactor control |
US3461109A (en) * | 1964-11-09 | 1969-08-12 | Phillips Petroleum Co | Process for the polymerization of conjugated dienes |
US3565873A (en) * | 1967-09-25 | 1971-02-23 | Copolymer Rubber & Chem Corp | Method and apparatus for polymerizing monomeric materials |
US3968090A (en) * | 1973-12-28 | 1976-07-06 | Mitsubishi Rayon Co., Ltd. | Method for removing heat of polymerization |
US4709111A (en) * | 1987-02-27 | 1987-11-24 | Uop Inc. | Oligomerization process with integrated heat utilization |
US5288823A (en) * | 1989-08-10 | 1994-02-22 | Phillips Petroleum Company | Chromium compounds and uses thereof |
US5198563A (en) * | 1989-08-10 | 1993-03-30 | Phillips Petroleum Company | Chromium compounds and uses thereof |
US5550305A (en) * | 1991-10-16 | 1996-08-27 | Amoco Corporation | Ethylene trimerization |
US5382738A (en) * | 1991-12-13 | 1995-01-17 | Phillips Petroleum Company | Chromium compounds and uses in trimerization or oligomerization |
US5541270A (en) * | 1993-05-20 | 1996-07-30 | Bp Chemicals Limited | Polymerization process |
US6825297B1 (en) * | 1999-05-14 | 2004-11-30 | The Dow Chemical Company | Transition metal complexes and olefin polymerization process |
US20040116758A1 (en) * | 2002-09-25 | 2004-06-17 | De Boer Eric Johannes Maria | Catalyst systems for ethylene oligomerisation to linear alpha olefins |
US20040122271A1 (en) * | 2002-09-25 | 2004-06-24 | Van Zon Arie | Process for making a linear alpha-olefin oligomer using a heat exchanger |
Cited By (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20040122271A1 (en) * | 2002-09-25 | 2004-06-24 | Van Zon Arie | Process for making a linear alpha-olefin oligomer using a heat exchanger |
US7994376B2 (en) | 2004-02-19 | 2011-08-09 | Chevron Phillips Chemical Company Lp | Olefin oligomerization |
US7820581B2 (en) | 2004-02-20 | 2010-10-26 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US8329608B2 (en) | 2004-02-20 | 2012-12-11 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US9550841B2 (en) | 2004-02-20 | 2017-01-24 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US8993822B2 (en) | 2004-02-20 | 2015-03-31 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US20100222577A1 (en) * | 2005-07-21 | 2010-09-02 | Chevron Phillips Chemical Company Lp | Diimine Metal Complexes, Methods of Synthesis, and Methods of Using in Oligomerization and Polymerization |
US20080004459A1 (en) * | 2005-07-21 | 2008-01-03 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US20080004441A1 (en) * | 2005-07-21 | 2008-01-03 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US7977269B2 (en) | 2005-07-21 | 2011-07-12 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US20070112150A1 (en) * | 2005-07-21 | 2007-05-17 | Small Brooke L | Diimine metal complexes, methods of synthesis, and method of using in oligomerization and polymerization |
US7728160B2 (en) | 2005-07-21 | 2010-06-01 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US7728161B2 (en) | 2005-07-21 | 2010-06-01 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and methods of using in oligomerization and polymerization |
US7727926B2 (en) | 2005-07-21 | 2010-06-01 | Chevron Phillips Chemical Company Lp | Diimine metal complexes, methods of synthesis, and method of using in oligomerization and polymerization |
US7910670B2 (en) | 2005-08-19 | 2011-03-22 | Chevron Phillips Chemical Company Lp | Methods of preparation of an olefin oligomerization catalyst |
US7902415B2 (en) | 2007-12-21 | 2011-03-08 | Chevron Phillips Chemical Company Lp | Processes for dimerizing or isomerizing olefins |
US9586872B2 (en) | 2011-12-30 | 2017-03-07 | Chevron Phillips Chemical Company Lp | Olefin oligomerization methods |
US10214463B2 (en) | 2014-09-22 | 2019-02-26 | Mitsubishi Chemical Corporation | Production method and production apparatus of α-olefin oligomer |
US9944661B2 (en) | 2016-08-09 | 2018-04-17 | Chevron Phillips Chemical Company Lp | Olefin hydroboration |
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ZA200502082B (en) | 2005-11-30 |
CA2499887A1 (en) | 2004-04-08 |
JP4498926B2 (en) | 2010-07-07 |
CN1735576A (en) | 2006-02-15 |
CN100519491C (en) | 2009-07-29 |
ATE432248T1 (en) | 2009-06-15 |
ES2324030T3 (en) | 2009-07-29 |
RU2005112253A (en) | 2005-09-10 |
EP1546069A1 (en) | 2005-06-29 |
AU2003271645A1 (en) | 2004-04-19 |
DE60327784D1 (en) | 2009-07-09 |
JP2006500411A (en) | 2006-01-05 |
RU2312848C2 (en) | 2007-12-20 |
CA2499887C (en) | 2011-08-16 |
WO2004029012A1 (en) | 2004-04-08 |
EP1546069B1 (en) | 2009-05-27 |
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