CA2556323A1 - Olefin oligomerization - Google Patents

Abstract

Provided is a method of oligomerizing alpha olefins. In an embodiment, an oligomerization catalyst system is contacted in at least one continuous reactor with a feed comprising olefins; an effluent comprising product olefins having at least four carbon atoms is withdrawn from the reactor; the oligomerization catalyst system comprises iron or cobalt, or combinations thereof; and the single pass conversion of ethylene is at least about 40 weight percent among product olefins having at least four carbon atoms. In another embodiment, the single pass conversion of ethylene comprises at least about 65 weight percent among product olefins having at least four carbon atoms. In another embodiment, product olefins of the effluent having twelve carbon atoms comprise at least about 95 weight percent 1-dodecene. In another embodiment, product olefins comprise at least about 80 weight percent linear 1-alkenes. In another embodiment, product olefins comprise at least about 20 weight percent alpha olefins having from about 8 to about 20 carbon atoms. In another embodiment, the oligomerization catalyst system provided comprises a selective 1-hexene (S1H) catalyst.

Description

OLEFIN OLIGOMERIZATION
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] The content of this application is related to the content of patent application number 10/379,828, filed March 4, 2003, entitled "Composition and Method for a Hexadentate Ligand and Bimetallic Complex for Polymerization of Olefins," which is incorporated herein by reference.
STATEMENT REGARDING FEDERALLY SPONSORED
RESEARCH OR DEVELOPMENT

[0002] Not applicable.
REFERENCE TO A MICROFICHE APPENDIK

[0003] Not applicable.
FIELD OF THE INVENTION

[0004] This invention generally relates to ethylene oligomerization to alpha olefins.
BACKGROUND OF THE INVENTION

[0005] Olefins, also commonly known as alkenes, are important items of commerce. Their many applications include employment as intermediates in the manufacture of detergents, as more environmentally friendly replacements where refined oils might otherwise be used, as monomers, and as intermediates for many other types of products. An important subset of olefins are olefin oligomers, and one method of making olefin oligomers is via oligomerization of ethylene, which is a catalytic reaction involving various types of catalysts.

[0006] Examples of catalysts used commercially in polymerization and oligomerization of olefins include alkyialuminum compounds, certain nickel-phosphirze complexes, and a titanium halide with a Lewis acid, such as diethylaluminum chloride. Some examples of catalysts, and in particular transition metal catalysts, employed in ethylene polymerization and oligomerization may be found in patent numbers 5,955;555, 6,103,946, WO 031011876, US
200210028941, WO
02/2805, and WO O1/ 58874, which are incorporated herein by reference.

[0007] Selective I-hexene (S1H) catalysts are another example of catalysts employed in the production of olefins. SIH catalysts are designed to be selective, for producton of 1-hexene.
Examples of such S1H catalysts may be found in patent numbers 6,455,648, 6,380,451, 5,986,153, 5,919,996, 5,859,303, 5,856257, 5,814,575, 5,786,431, 5,763,723, 5,689,028, 5,563,312, 5,543,375, 5,523,507, 5,470,926, 5,45I,645, and 5,438,027, which are incorporated herein by reference.
[0408] Applications and demand for olefin polymers and oligomers continue to multiply, and competition to supply them correspondingly intensifies. Thus, additional novel and improved catalysts, and methods of olefin polymerization and oligomerization, are desirable.
SUMMARY OF THE INVENTION
[0009] Provided is a method of oligomerizing alpha olefins. In an embodiment, an oligomerization catalyst system is contacted in at least one continuous reactor with a feed comprising olefins; an effluent comprising product olefins having at least four carbon atoms is withdrawn from the reactor; the oligomerization catalyst system comprises iron or cobalt, ox combinations thereof; and the single pass conversion of ethylene is at least about 40 weight percent among product olefins having at least four carbon atoms. In another embodiment, the single pass conversion of ethylene comprises at least about 65 weight percent among product olefins having at least four carbon atoms. In another embodiment, product olefins of the effluent having twelve carbon atoms comprise at Ieast about 95 weight percent 1-dodecene. In another embodiment, 'product olefins comprise at least about 80 weight percent linear 1-alkenes.
In another embodiment, product olefins comprise at least about 20 weight percent alpha olefins having from about ~ to aboui 20 carbon atoms. In another embodiment, the oligomerization catalyst system provided comprises a selective 1-hexene (SlI3) catalyst.
[0010] In an embodiment, the oligomerization catalyst system provided comprises a metal complex activated by a co-catalyst wherein the metal complex comprises a ligand having chemical structure I:
1~
R
1~
I
The components of the ligand having chemical stricture I, labeled RI through R', may be defined as follows:

Rl, R2, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, an inert functional group, or any two of Rl-R3, vicinal to one another, taken together may form a ring;
R4 and RS are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or inert functional group;
' R6 and R' are each independently aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, optionally substituted aryl group in combination with and Tj coordinated to a metal, optionally substituted aromatic hydrocarbon ring, or optionally substituted polyaromatic hydrocarbon moiety.
[0011] Also provided is an oligomerization method comprising an oligomerization catalyst system contacted with a feed comprising olefins in at least one continuous reactor; a reactor effluent comprising product olefins having at least four carbon atoms; a single pass conversion of ethylene of at least about 65 weight percent among product olefins having at least four carbon atoms; and at least about 95 weight percent 1-dodecene among product olefins having twelve carbon atoms. In an embodiment, the oligomerization catalyst system comprises a metal alkyl or metal hydride species. In another embodiment, the at least one continuous reactor comprises a temperature of from about 40 to about 150 degrees Celsius. Tn another embodiment, the at least one continuous reactor comprises a loop reactor where fluid flow comprises a Reynolds number of from about 200,000 to about 700,000. In another embodiment, the at least one continuous reactor comprises a tubular reactor where fluid flow comprises a Reynolds number of from about 300,000 to about 2,000,000.

BRIEF DESCRIPTION OF THE DRAWINGS
[0012] Fig. 1 illustrates an embodiment of an oligomerization reactor in accordance with the method provided.
[0013] Fig. 2 illustrates an embodiment of a process design for simultaneous employment of combinations of catalysts in parallel reactors.
1[0014] Fig. 3 illustrates an embodiment of a process design for simultaneous employment of combinations of catalysts in the same reactor.
[0015] Fig. 4 illustrates an embodiment of a process design for consecutive employment of catalysts.
[0016] Fig. 5 illustrates an embodiment of a process design in accordance with the oligomerization provided.
[0017] Fig. 6 illustrates l~-hexene quality for several embodiments of the oligomerization provided.
[0018] Fig. 7 illustrates 1-octene quality for several embodiments of the oligomerization provided.
[0019] Fig. 8 illustrates changes in paraffin content over time while executing an embodiment of the oligomerization provided.
[0020] Fig. 9 illustrates 1-hexene purity for several embodiments of the oligomerization provided.
(0021] Fig. 10 illustrates 1-octene purity for several embodiments of the oligomerization provided.

DETAILED DESCRIPTION OF THE INVENTION
[0022] Fig. 1 illustrates an embodiment of a method for oligomerization of alpha olefins. A
feed 10 comprising olefins may be contacted with an oligomerization catalyst system. In an embodiment, the oligomerization catalyst system comprises iron or cobalt. In another embodiment, the feed 10 comprises ethylene. Oligornerization of the feed 10 may take place in a continuous reactor 20, and an oligomerization reactor effluent 30 including at least three components is withdrawn from the reactor 20. The components of the oligomerization effluent 30 may comprise diluent, product olefins, any ethylene not consumed by oligomerization, and catalyst system constituents. Product olefins of the effluent 30 comprise olefins having at least four carbon atoms thaf are produced by the oligomerization reaction in the reactor 20. In an embodiment, .
product olefins of the effluent 30 comprise alpha olefins having at least four carbon atoms that are produced by the oligomerization reaction in the reactor 20. The diluent comprises the remaining components of the effluent 30, other than product olefins, ethylene, and catalyst system constituents.
[0023] In an embodiment, oligomerization to product olefins having at least four carbon atoms comprises a single pass conversion of ethylene of at least about 40 weight percent. The single pass conversion may be expressed as the weight percent of reactant in the feed, e.g., ethylene, that is oligomerized during a single pass through the reactor. By calculation, the single pass conversion of ethylene may be the ratio, expressed as a percentage, of the mass of product olefins in the effluent divided by the mass of ethylene in the feed. The single pass conversion may also be expressed as the probability, expressed as a percentage, that one molecule of reactant in the feed, e.g., ethylene, will be oligomerized in the course of a single pass through the reactor. In another embodiment, oligomerization of ethylene to product olefins having at least four carbon atoms comprises a single pass conversion of ethylene of at least about 50 weight percent. In another embodiment, the oligomerization comprises a single pass conversion of ethylene of at least about 65 weight percent. Jn another embodiment, the oiigomerization comprises a single pass conversion of ethylene of at least about 75 weight percent. In another embodiment, the oligomerization 'comprises a single pass conversion of ethylene of at least about 85 weight percent.
[0024] ~n addition to ethylene . conversion, product quality and purity characterize the oligomerization described herein. In an embodiment, the effluent froth the oligomerization reactox includes product olefins having at least four carbon atoms that comprise at least about 80 weight percent linear I-alicenes. In another embodiment, the effluent from the oligomerizatioz~ reactor includes from about 25 to about 95 weight percent product olefins having at least four carbon atoms. Tn another embodiment, the eft3uent includes at least about 40 weight percent product olefins having at least four carbon atoms. in another embodiment, the eft3uent includes from about 30 to about 80 weight percent product olefins having at least four carbon atoms. In another embodiment, the effluent includes from about G~0 to about 70 weight percent product olefins having at least four caxbon atoms. In another embodiment, the effluent zncludes from about 45 to about 65 weight percent product olefins having at least four carbon atoms. In another embodiment, the effluent includes from about 50 to about 60 weight percent product olefins having at least four carbon atoms. In another embodiment, the effluent comprises from about SO to about 90 weight percent product olefins having at least four carbon atoms. In another embodiment, the effluent comprises from about 60 to about 90 weight percent product olefins having at least four carbon atoms. In another embodiment, the effluent comprises from about 70 to about 85 weight percent product olefins having at least four carbon atoms.
[0025] In an embodiment of the oligomerization, product olefins having at least four carbon atoms comprise olefins having from about 8 to about 20 carbon atoms. ~ In another embodiment, product olefins having at least four carbon atoms comprise at least about 20 weight percent olefins having from about 8 to about 20 carbon atoms. In another embodiment, product olefins having at least four carbon atoms comprise at Ieast about 30 weight percent olefins having from about 8 to about 20 carbon atoms. In another embodiment, product olefins having at least four carbon atoms comprise at least about 40 weight percent olefins having from about 8 to about 20 carbon atoms.
In another embodiment, product olefins having at least four carbon atoms comprise at least about 20 weight percent olefins having from about 6 to about 20 carbon atoms. In another embodiment, product olefins having at least four carbon atoms comprise at least about 35 weight percent olefins having from about 6 to about 20 carbon atoms. In another embodiment, product olefns having at least four carbon atoms comprise at least about 50 weight percent olefins having from about 6 to about 20 carbon atoms. In another embodiment, product olefins having at least four carbon atoms comprise at least about 60 weight percent olefins having from about 6 to about 20 carbon atoms.
[0026] Selectivity for hexene may be of interest among the product olef ns. In an embodiment, product olefins comprise at least about 20 weight percent olefins having 6 carbon atoms. In another embodiment, product olefins comprise from about 25 to about 70 weight percent olefins having 6 carbon atoms. In another embodiment, product olefins comprise from about 30 to about 60 weight percent olefins having 6 caxbon atoms. In another embodiment, product olefins comprise from about 40 to about 50 weight percent olefins having 6 carbon atoms. In another embodiment, of the product olefins having 6 carbon atoms, at least about 98 weight percent are 1-hexene.
[0027] The purity of octenes and dodecenes among product olefins may also be of interest. In an embodiment, product olefins having 8. carbon atoms comprise at Ieast about 95 weight percent 1-octene. In another embodiment, product olefins having 8 carbon atoms comprise at least about 96 weight percent 1-octene. In another embodiment; product olefins having 8 carbon atoms comprise at least about 97 weight percent 1-octene. In another embodiment, product olefins having 8 carbon atoms comprise at least about 98 weight percent 1-octene. In another embodiment, product olefins having 8 carbon atoms comprise at least about 99 weight percent 1-octene. In another embodiment, product olefins having 12 carbon atoms comprise at least about 93 weight percent 1-dodecene. In another embodiment, product olefins having 12 carbon atoms comprise at least about 95 weight percent 1-dodecene. In another embodiment, product olefins having 12 carbon atoms comprise at least about 96 weight percent 1-dodecene.
In another embodiment, product olefins having 12 carbon atoms comprise at least about 97 weight percent 1-dodecene. In another embodiment, product olefins having 12 carbon atoms comprise at least about 98 weight percent 1-dodecene.
j0028] An oligomerization catalyst system is employed in the oligomerization provided. The oligomerization catalyst system may be homogeneous, heterogeneous, supported, or unsupported, as those terms are known in the art. In an embodiment, the oligomerization catalyst system comprises a co-catalyst, and a ligand complexed with a metal. In another embodiment, the oligomerization catalyst system comprises a metal complex activated by a co-catalyst, Wherein the metal complex comprises a ligand having chemical structure I:

:1 r~
I
The components of the ligand having chemical structure I, labeled Rl through R', may be defined as follows:
Rl, RZ, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, an inert functional group, or any two of R'-R3, vicinal to one another, taken together may form a ring;
R4 and RS are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or inert functional group;
R6 and R' are each independently aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, optionally substituted aryl group in combination with and Tj coordinated to a metal, optionally substituted aromatic hydrocarbon ring, or optionally substituted polyaromatic hydrocarbon moiety.
[0029] The metal complex provided may be formed by complexing a ligand, .such as, for example, the ligand having chemical structure I, with a metal. In an embodiment, the metal selected for compIexing with a ligand to form the metal complex provided comprises a transition metal. In other embodiments, the metal selected to form the metal complex comprises iron, nickel, palladium, cobalt, vanadium, chromium, or combinations thereof. In another embodiment, the metal comprises iron, cobalt, or combinations thereof. In another embodiment, the oligomerization catalyst system comprises chromium.
[0030] Other variations on the oligomerization catalyst system are presented.
For example, the 'order of addition of reagents may vary. In an embodiment, activating the metal complex, occurs in the absence of ethylene. .
(003I] Refernng to chemical structure I, the configuration of the ligand may vary with selection of Rl through R~. In an embodiment, Rl - R~ are selected such that the ligand having chemical structure I is symmetrical. A symmetrical ligand as provided herein is symmetrical if it possesses symmetry higher than 'C1' symmetry, where Cl refers to the C~ point group. In an embodiment, RI - R' are selected such that the ligand having chemical structure I is asyrrimetrical.
An asymmetrical ligand as provided herein is asymmetrical if it possesses only 'C1' symmetry, i.e., possesses no mirror plane, no rotational axis of symmetry, and no inversion center.
[0032] The oligomerization catalyst system further comprises a co-catalyst, which may be involved in catalyst activation. In an embodiment, the co-catalyst comprises a metal alkyl or metal hydride species. In another embodiment, the co-catalyst comprises one or more Lewis acids; a combination of one or more Lewis acids .and one or more alkylating agents; one or more alkyl aluminum compounds; one or more alkyl aluminoxanes; methyl aluminoxane (MAO);
modified MAO; tri-alkyl aluminum; diethylaltuninum chloride (DEAC); or combinations thereof. In another embodiment, the co-catalyst comprises triethylaluminum (TEA), trimethylaluminum (TMA), tri-isobutyl aluminum (TIBA), tri-butyl aluminum, or combinations thereof. In an embodiment, where the catalyst system comprises an iron catalyst, the molar ratio of aluminum to iron in the oligomerization ranges from about 1:1 to about 10,000:1. In another embodiment, ,where the catalyst system comprises an iron catalyst, the molar ratio of aluminum to iron in the oligomerization ranges from about 100:1 to about 3,000:1. In another embodiment, where the catalyst system comprises an iron catalyst, the molar ratio of aluminum to iron in the nligomerization ranges from about 200:1 to about 2,000:1.
[0033 Components of the oligomerization catalyst system may vary. In an embodiment, the oligomerization catalyst system comprises a metal complex activated by a co-catalyst, wherein the metal complex comprises a ligand having chemical structure II:
R~
Rs / R1 R5 \ ~ Ra N N
W'~10 30\
Y
z X60 40~
N N
t N0 i R5 ~ ~ ~ Ra R3 ~ .R1 II
The components of the ligand having chemical structure II, labeled Rl - R5, W, Y, and Z, may be defined as follows:
Rl , Rz , and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or an inert functional group;

R4 and RS are each independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl;
Y is a structural bridge, and W, Y, and Z independently comprise hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl having from about 0 to about 30 carbon atoms.
[0034) In another embodiment of the oligomerization catalyst system, a metal complex is activated by a co-catalyst, wherein the metal complex may include a ligand having chemical structure III:

~q III
The components of the ligand having chemical structure III, labeled Rl - R5, Zl, and Z2, may be defined as follows:
R1-RS each comprzse, independently, hydrogen, optionally substituted hydrocarbyl, an inert functional group, or any two of Rl-R3 vicinal to one another taken together may form a nng;
Z1, which is different from Z~, is an aryl or substituted aryl group; and N

Zz comprises an aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, or an optionally substituted aryl group in combination with and ~ coordinated to a metal.
[0035] In another embodiment of the ligand having chemical structure III, Z2 may be defined as an aryl, substituted aryl, optionally substituted aromatic heterocyclic moiety, an optionally substituted polyaromatic heterocyclic moiety, an optionally substituted aliphatic heterocyclic moiety, or an optionally substituted aliphatic heterohydrocarbyl moiety.
[0036] In another embodiment of the oligomerization catalyst system, a metal complex is activated by a co-catalyst, wherein the metal complex may include a ligand having chemical structure IV:
1~~
~'?

~s IV
The components of the ligand having chemical structure IV, labeled RI - R15 and A~ - Ag, may be defined as follows:
A~-A6 each comprise, independently, carbon, nitrogen, oxygen, or sulphur;

in the absence of A6, A1 may be directly bonded to A5;
Ri-Ria, Ri4-Ris, and, if present, R13, are each, independently, hydrogen, optionally substituted hydrocarbyl, or an inert functional group;
any two of Rl-R15, vicinal to one another, taken together may form a ring; and conditionally, when Al-AS and Ab, if present, are all carbon, said atoms constitute the ~cyclopentadienyl or aryl part of a Tj coordinated metal.
[0037] Tn another embodiment of the oligomerization catalyst system, a metal complex is activated by a co-catalyst, wherein the metal complex may include a ligand having chemical structure V
~3 V
The components of the ligand having chemical structure V, labeled RI - RS and Z, may be defined as follows:
Rl-RS are each, independently, hydrogen, substituted hydrocarbyl, an inert functional group, or any two of Rl-R3, vicinal to one another, taken together may form a ring; and each Z, selected independent of the other, is a substituted aryl, an optionally substituted polyaromatic hydrocarbon moiety, an optionally substituted heterohydrocarbyl moiety, or a substituted aryl group in combination with a metal, said optionally substituted aromatic hydrocarbon ring being Tj coordinated to the metal.
[0038] In another embodiment of the oligomerization catalyst system, a metal complex is activated by a co-catalyst, wherein the metal complex may include a ligand having chemical structure VI:

R2 / ~ R3 R4 w ~ R5 Rs ~ N ~ R15 R7 ~ N N ~ R1~.
R ~ ~ R R ' ~ R

Rg R12 VI
The components of the ligand having chemical structure VI, labeled R1 - RCS, may be defined as follows:
Rl-Rs and R~-R9 and R12-RI4 are each, independently, hydrogen, substituted hydrocaxbyl, an inert functional group, or any two of R;-R3, R~-R9, and R12-Rla, vicinal to one another, taken together may form a ring; and R6, Rio, Rli, and Rls are identical and are selected from fluorine or chlorine.
[0039] In another embodiment of the oligomerization catalyst system, a metal complex is activated by a co-catalyst, wherein the metal complex may include a ligand having chemical structure VII:

VII
The components of the ligand having chemical structure VII, labeled Rl - Rts, may be defned as follows:
Ri-RS and R~-R9 and Ri2-R14 are each, independently, hydrogen, substituted hydrocarbyl, an inert functional group, or any two of Rl-R3, R~-R9, and R12-Ria, vicinal to one another, taken together may form a ring;
Rb is hydrogen, substituted hydrocarbyl, an inert functional group, or taken together with R~ or Rø to form a ring;
Rlo is hydrogen, substituted hydrocarbyl, an inert functional group, or taken together with R9 or Rd to form a ring; and Rl ~ and Rls are each, independently, hydrogen or an inert functional group.
(0040] The oligomerization catalyst system may include combinations of catalysts, which may modify the distribution of product olefins in the effluent. In an embodiment, the oligomerization catalyst system comprises a selective one hexene (S1H) catalyst. In another embodiment, the oligomerization catalyst. system comprises a SIH catalyst; a metal complex including a ligand having chemical structure I, lI, IQ, IV, V, VI, or VII, or combinations thereof, as provided herein;
and at least one co-catalyst. In an embodiment where a combination of catalysts makes up the oligomerization catalyst system, an S 1H catalyst; a metal complex including a ligand having chemical structure I, II, III, IV, V, VI, or VII, or combinations thereof; and said co-catalyst may be employed simultaneously. Fig. 2 ~ illustrates an embodiment of a process design where combinations of different catalysts and co-catalysts may be employed simultaneously. A transition metal catalyst oligomerization may be executed'in a first reactor 200, and simultaneously a S1H
catalyst oligomerization may be executed in a parallel reactor 210.
Alternatively, two different transition metal catalysts may be employed simultaneously in the two parallel reactors 200, 210, or a combination of transition metal and S1H catalysts may be employed simultaneously in the two parallel reactors 200, 210. The effluents 205, 215 of the reactors 200, 210 may be combined into a single process output stream 220. Fig. 3 illustrates another embodiment of a process design for simultaneous employment of combinations of transition metal and S1H catalysts and co-catalysts.
Combinations of different transition metal catalysts, or combinations of transition metal catalysts and S1H catalysts, may be employed in the same reactor I00. Thus, the effluent 110 would include product olefins generated by each of the oligomerization catalysts employed in the reactor 100.
[0041] In another embodiment where a combination of catalysts makes up the oligomerization catalyst system, an S1H catalyst; a metal complex including a Iigand having chemical structure I, II, III, IV, V, VI, or VII, or combinations thereof; and said co-catalyst may be employed consecutively. Fig. 4 illustrates an embodiment of a process design where catalysts may be employed consecutively. One type of oligomerization catalyst or combination of catalysts may be employed in a first reactor 300, and a second type of oligomerization catalyst or combination may be employed in a second reactor 310. The first 300 and second 310 reactors are operated in series.
The first reactor effluent 305 is fed to the second reactor 310, so the second reactor effluent 315 'comprises a mixture of the two reactor effluents 305, 3I5.
[0042] The particular combination of catalysts employed in a particular process design, such as, for example, those combinations and designs illustrated by Figs. 2 - 4, may modify the distribution of product olefins in the effluent of an oligomerization process.
Such a modification may cause the distribution of product olefins to vary from a typical Schulz-Flory distribution, and, therefore, also adjust the Schulz-Flory constant, or K-value associated with such a product olefin distribution. In an embodiment where an oligomerization catalyst system comprises a combination of catalysts, the product olefins of the oligomerization comprise a 1-hexene content of from about 20 to about 80 weight percent. In another embodiment, product olefins comprise a 1-hexene content of from about 50 to about 80 weight percent.
j0043] The lifetimes of the components of the oligomerization catalyst system may vary. For example, the lifetime of a catalyst including a metal complex may be different than the lifetime of an S1H-type catalyst. Thus, designing the oligomerization method as provided herein to account for such variances may be advantageous. In an embodiment, where the continuous reactor includes a tubular reactor, the oligomerization catalyst system is inj ected at more than one point along the length of the reactor. In another embodiment, a metal complex is injected at more than one point along the length of the reactor. In another embodiment, the oligomerization catalyst system and olefins are injected at more than one point along the length of the reactor.
[0044] The oligomerization provided may be a continuous process carried out in one or more reactors. In. an embodiment, the reactor comprises a loop reactor, tubular reactor, continuous stirred tank reactor (CSTR), or combinations thereof.
'(0045] The oligomerization may be further characterized by the velocity of reaction components in the continuous reactor, and associated Reynolds numbers. In an embodiment, the continuous reactor may be a loop reactor where fluid flow in the loop reactor comprises a Reynolds number of from about 100,000 to about 1,000,000. In another embodiment, the continuous reactor may be a loop reactor where fluid flow in the loop reactor comprises a Reynolds number of from about 200,000 to about 700,000. In another embodiment, the continuous reactor may be a tubular reactor where fluid flow in the tubular reactor comprises a Reynolds number of from about 100,000 to about 10,000,000. In another embodiment, the continuous reactor may be a tubular reactor where fluid flow in the tubular reactor comprises a Reynolds number of from about 300,000 to about 2,000,000.
(0046] In various embodiments, the continuous reactor may be employed in the form of different types of reactors in combination, and in various arrangements. In an embodiment, the continuous reactor may be a combination of a tubular reactor and a CSTR. In other embodiments, the continuous reactor may be employed as xeactors in series, reactors in parallel, or combinations thereof. In an embodiment, the continuous reactor may be more than one CSTR in series. In another embodiment, the continuous reactor may be a tubular reactor and a loop reactor in series.

[0047] It is known in the art that the temperatures associated with oligomerization may vary depending on the oligomerization catalyst system employed. For example, oligomerizations employing transition metal catalysts typically involve lower temperatures.
Such lower reactor temperatures, however, may make precipitation of waxes and, therefore, plugging more problematic. Such waxes that cause plugging may be, for example, the insoluble portion of wax products from the oligomerization reaction that have at Ieast 20 carbon atoms.
The turbidity, or clarity of the reactor contents upon. visual inspection may be an indicator of the presence of precipitated waxes. As the level of precipitated waxes in the reactor increases, the turbidity of the reactor contents also typically increases. Thus, lower reactor temperatures and potential increases in wax precipitation and plugging may be characteristic of oligomerization. Tn an embodiment, at least one oligomerization reactor comprises a temperature of from about 40 to about 150 degrees Celsius. In another embodiment, at Ieast one reactor comprises a temperature of from about 40 to about 90 degrees Celsius. In another embodiment, at least one reactor comprises a temperature of from about 80 to about 150 degrees Celsius. In another embodiment, the contents of the reactor at steady state, even without substantial turbulence, are not turbid.
[0048] A diluent, or solvent is among the components of the oligomerization.
At lower oligomerization temperatures, such as those associated with late transition metal catalysts, selection of diluent may contribute to prevention of wax precipitation and, therefore, affect the turbidity of reactor contents, and plugging. In embodiments, the diluent comprises aliphatics, non-aliphatics, aromatics, saturated compounds having from 4 to 8 carbon atoms, or combinations thereof. In other embodiments, the diluent comprises cyclohexane, heptane, benzene, toluene, xylene, ethylbenzene, or combinations thereof. In another embodiment, the diluent comprises an aromatic compound having from about 6 to about 30 carbon atoms. In another embodiment, the diluent comprises olefins. In another embodiment, the diluent comprises alpha olefins.
In another embodiment, the diluent comprises olefins having from about 4 to about 30 carbon atoms. Tn another embodiment, the diluent comprises olefins having from about 4 to about 12 carbon atoms.
In another embodiment, the diluent comprises olefins having from about 10 to about 30 carbon atoms. In another embodiment, the diluent comprises olefins having from about 12 to about 18 carbon atoms. In yet other embodiments, the diluent comprises 1-butene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1-octadecene, or combinations thereof. In another embodiment, the diluent comprises 1-tetradecene. In another embodiment, the diluent comprises no more than about 30 weight percent of the oligomerization reactor effluent. In another embodiment, the diluent comprises no more than about 20 weight percent of the reactor effluent. In another embodiment, the diluent comprises no more than about 10 weight percent of the reactor effluent.
[0049] As is known in the art, coolants may be employed when operating oligomerization reactors. For example, vaporized water may be used to cool an oligomerization reactor.
Accordingly, as oligomerization temperature may vary with the type of catalyst employed, so may the coolant employed to cool the reactor. In an embodiment, a coolant more volatile than water is used in cooling the continuous reactor. In another embodiment, the coolant employed comprises butane, isobutane, isopentane, or combinations thereof.
[0050] Reactor, or ethylene pressure may impact the product olefins of the oligomerization. In an embodiment, the distribution of product olefins in the effluent is manipulated via modifying reactor pressure. In an embodiment, where reactor pressure is modified in order to manipulate product olefin distribution, the oligomerization catalyst system includes a transition metal complex and a ca-catalyst, and the co-catalyst is a tri-alkyl aluminum.
[0051] Further provided is a method that comprises contacting a feed comprising olefins and an oligomerization catalyst system. The feed is oligomerized in at least one continuous reactor, and an effluent comprising product olefins that have at least four carbon atoms is withdrawn from 'the reactor. In an embodiment, the method of oligomerization to product olefins having at least four carbon atoms is further characterized by a single pass conversion of ethylene of at least about 65 weight percent. Additionally, the product olefins from the oligomerization that have twelve carbon atoms comprise at least about 95 weight percent 1-dodecene.
[0052] In embodiments of the method comprising a single pass conversion of ethylene of at least about 65 weight percent, and product olefins having twelve carbon atoms that comprise at least about 95 weight percent 1-dodecene, the oligomerization catalyst system may comprise a metal complex activated by a co-catalyst where the metal complex comprises a ligand having one or more of chemical structures I - VIII, or combinations thereof In another embodiment, the oligomerization catalyst system may comprise an S1H catalyst. In other embodiments, the oligomerization catalyst system may comprise iron, cobalt, chromium, nickel, vanadium, or combinations thereof.
(0053] The present application further discloses a method of oligomerizing alpha olefins where a metal complex having chemical structure VTII is contacted with a co-catalyst and a feed comprising olefins.

Rs / R~
R5 \ ~ Ra I .N
--N~ ~ i _N' _ _M2, -IN
N
R5 ~ ~ ~ R4 Ra R~
R~
VITI
[0054] The metal complex having chemical structure VIII may be produced from a ligand having chemical structure II as provided herein. The metal complex VIII may be formed as a result of a coordination reaction between the ligand II and a metal salt. In an embodiment, the components of the metal complex of chemical structure VIII, labeled as Rl -R5, W, Y, Z, M, and Xn are as follows:
wherein RI, RZ , and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or an inert functional group;
R4 and RS are each independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl; and Y is a structural bridge, and W, Y, and Z are independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl having from about 0 to about 30 carbon atoms.
wherein M, and MZ are metal atoms that are independently selected from a group comprising cobalt, iron, chromium, and vanadium;
each X is an anion; and n is 1, 2, or 3, so that the total number of negative charges on X is equal to the oxidation state of Ml or Mz .
EXAMPLES
[0055] The following examples, 1 through 3, are merely representative of aspects of the present invention and, as one skilled in the art would recognize, the present invention may be practiced without many of the aspects illustrated by the examples. Data in examples 2 and 3 that represent process components, and compositions of reaction mixtures and products were deterinined by gas chromatography using a standard boiling point capillary column and flame ionization detector (GC/Fff~).

[0056] Several a.-olefin mixtures were mixed separately with two diluents, cyclohexane and 1-tetradecene. The level of diluent in each mixture was varied between 10 and 27 percent to simulate a reactor effluent, excluding unreacted ethylene, with from 90 to 73 percent product composition, respectively. The amounts of wax in the mixtures were gradually increased such that the total amount of wax in the mixtures ranged from 10 to 15 percent. The temperatures of the mixtures were then varied from 35 to 65°C for each mixtuxe, in order to determine when each mixture would become a clear solution.
[0057] Using a typical commercial Schulz-Flory chain growth factor of K = 0.7, where K = (moles C"+z)/{moles Cn), SOOg of a mixture containing 1358 of diluent (either cyclohexane or 1-tetradecene) and 365g of a-olefns were prepared in a 1L flask fitted with a heating mantle. A stirbar was added to the flask, which was sealed and then connected to a bubbler via a needle in order to relieve pressure. Due to the volatility of 1-butene and 1-hexene, their masses were combined with the mass of 1-octene for preparing the solutions, such that 1-octene was used to simulate the presence of 1-butene, 1-hexene and 1-octene (see Table 1). Similarly, 1-dodecene was used to represent the Clo, Cl2a ~d C14 fractions, and 1-octadecene was used to represent the Ci6 and Cl8 fractions.
For the waxes, Cap/24~
C26/28~ ~d C3o were chosen to represent the wax products made by the catalysts of interest. In addition to these two mixtures, a third mixture was prepared in which only SOg of 1-tetradecene diluent was used in 506g of the mixture.
[005$] The three prepared mixtures, shown in columns 1 - 3 in Table 1, were then heated slowly with rapid stirring to determine the point at which each solution became clear. For the solution containing 73 percent product olefins and 27 percent Cla diluent, the solution became clear at 55°C (col. 1), and when the diluent concentration was lowered to 10.3 percent (col. 3), the solution became clear at 60°C. Contrasting these results, the mixture containing cyclohexane (col.
2) did not become clear under any of the temperature conditions studied. The results would suggest that a mid-range a-olefin fraction, such as 1-tetradecene, may be a better solvent and less likely to promote reactor plugging than cyclohexane. Also, the high level of product in the effluent suggests that it may be possible to run an oligomerization of this sort at low temperatures and high conversions without causing lines to plug.
[0059] To test the limits of reactor composition, further experiments were performed in which the amount of wax in the reactor was artificially inflated. Columns 4, 5, and 6 in Table 1 illustrate the respective changes that were made to solutions 1, 2, and 3. In each mixture the amount of diluent and non-wax olefins was held constant, but the amount of CZO+ waxes was increased by about 30 percent. As expected, the cyclohexane mixture 5 was cloudy at all of the temperatures studied. However, the 26 percent diluent (col. 4) and the 10 percent diluent (col. 6) mixtures were completely clear at 40 and 45°C, respectively. For solutions 1 and 3, the "clear" point was determined by slowly raising the temperature, but for solutions 4 and 6, the point of total clarity was determined by slowly lowering an. akeady elevated temperature.
[0060] As a final incremental change, solutions 7 and 8 were prepared, in which the amount of wax in solutions 4 and 6 was increased. In this case, a.Il of the additional wax was C3o or higher, so that the amount of higher molecular weight material could be exaggerated. With these elevated amounts of wax, the solutions were still clear at 40 and 45°C, respectively.
Table I
Component Mixture r (al dams)1 I 3 4 5 j 6 7 ~
2 ; 8 ;

j C8 ' ~ 227 ~ 227 ~ 227 j t C12 j 109 135 ~
~ Cyc h 109 [ 0 109 a ~ 13S 109 0 ; ~

~

~

j ~

j CI4 [ i SO ~ 0 a SO SO
I35 0 135 ~ I3S
, ~

j C18 i j 42 ; 39 ~ 42 42 ( i ~

C20/24 ~30 30 32 40 40 ! 43 43 , 40 i C26/28 ~ 9 9.2 j IZ ~ I2.7 12.7 9 ~ 12 j 12 j i C30 ~ I 11.2 14.614.61 ;22.4( ~ ~

Total (g) ~ 499 506 ~ 516 499 516 ;

~

( Diluent _ 27 IO ~ 26 ~ 10 9 ~ ~ 26 ( 26 27 ;

~% Wax t 10 10.3 112.912.913.5114.1 10 j 14.7 [ ~ r j ~

1 2 3 4 5 6 ~ 7 8 ~

T ~o~> ; ~i ~ J
I

3S - j a j a , b b !
a a b b ( ~

# tp, N
40 i ~ a ". a .. b a a ;.,~~{w~' b ~~:~
~ c; ~' 45 b ;a~ a Ic a '.,'' [ ' a 50 b i b j a ~ c [ j b c c c ;

SS ~ b b ~c a c ~ c i c ~ c '.

;~~.~
60 I ~ S a a ~ c ~ I
c b ca.~ i c c ~

r 6S ~ [ c i a ~ c [ [
c b c c c [ i [

a = very cloudy b = slightly cloudy c = totally clear (0061] Two specific iron catalysts were tested under semi-continuous operating conditions.
~'ig. 5 illustrates the process design for the test. 120g of solvent was pumped into a 1.0 L reactor under inert conditions, and the reactor was then pressurized with ethylene to either X00 or 1000 psig., Next, high pressure pumps were used to quickly transfer the first hour's amounts of catalyst, which was the iron dichloride complex of either structure 1X or X, and co-catalyst (TEA) to the reactor.
I \N I
Nw I,N \
Fe CI~ CI I /
IX
I N 11 I ~ 11 N~FI/N / \ N~Fe~N \
n~" / CI/ CI \ ~ I / CI CI
X
(0062] The catalyst was introduced as an anhydrous methylene chloride solution (O.lmg/ml), and the co-catalyst was diluted in anhydrous heptane. The reaction was allowed to exotherm to the run temperature of 50°C, and this temperature was maintained by internal cooling coils in the reactor. The catalyst and co-catalyst pumps were allowed to continue running at the hourly rates shown in Table 2, and the ethylene was fed "on demand" using a pre-set regulator. The reaction was periodically sampled via the sampling port, and the data in Table 2 were generated via GC
analysis. Entries 1 - 8 reflect data collected employing an iron catalyst formed from a ligand 'having chemical structure IX and FeClz, while Entry 9 reflects data collected under similar conditions but employing an iron catalyst formed from a ligand having chemical structure X and FeClz. The data shown for the product distributions and the product parities are from the last samples taken for each reaction, i.e. at the highest 'conversion level. Each reaction was run for approximately 3 hours after the reaction had exothermed to 50°C. The catalyst productivities in Table 2 are based on the total amount of product formed and the total amount of catalyst and co-catalyst fed to the reactor. The' cyclohexane solvent was used as the internal standard for calculating the catalyst productivities.
Table 2 Entry 1 2 3 4 5 6 7 8 9 Solvent (120g) C6HlzC(H12CsHizC6H12C6HIZC6HizCsHiz1-ButeneC6Hlz Catalyst IX IX IX IX IX IX IX IX X

Flowrate (mg/hr) 0.4 0.4 0.2 0.2 0.4 0.4 0.2 0.2 0.2 Yield (g) of product322 214 459 326 329 343 118 312 374 AOs lb prod/lb Al 4464 2321 5200 6170 3193 2997 1518 4227 5004 lb prod/lb Fe cat 224 116 521 620 321 301 76 424 509 (x103) TEA:Fe ratio 1000 1000 2000 2000 2000 2000 1000 2000 2000 K(C20/C18) 0.68 0.77 0.67 0.74 0.68 0.78 0.76 0.69 0.68 K(C16/C14) 0.68 0.76 0.69 0.76 0.68 0.78 0.77 0.69 0.69 K(C10/C8) 0.68 0.76 0.67 0.76 0.68 0.78 0.77 0.69 0.69 P ethylene (psig) 500 1000 500 1000 500 1000 1000 500 500 1-C6 Purity 99.3599.1699.3499.2699.2998.8898.9798.87 99.34 C6 % branched AO 0.16 0.03 0.19 0.14 0.16 0.07 0.03 0.47 0.17 C6 % Paraffin 0.24 0.29 0.19 0.15 0.38 0.27 0.38 0.19 0.21 1-C8 Purity 99.13 99.16 99.07 99.45 99.17 98.69 98.98 98.27 . 99.05 C8 % branched AO 0.30 0.25 0.32 0,24 0.29 0.66 0.27 0.83 0.29 [0063] In examining Table 2, some additional observations are noted. First, the product distribution, as expressed by the Schulz-Flory K value, was approximately 0.67 - 0.69 at 500 psig.
ethylene pressure, and reflected pressure dependence. Upon increasing the pressure to 1000 psig, 'the K value increased to 0.75 - 0.77 (compare entries 1 and 2). Also, using the data in entry 3 of Table 2, Figs. 6, 7, and 8 were created. Fig. 6 shows that when increasing the concentration of 1-butene in the reactor, the 1-hexene quality remains near 99.3 percent at 12 percent 1-butene concentration. Fig. 7 shows that the I-octene purity remains over 99 percent with 25 percent 1-butene and 1-hexene in the reactor. Fig. 8 illustrates how the overall paraffin content in the reactor decreases with increasing conversion and run length.

[0064] The tests described in entry 8 of Example 2 are furthered described in Example 3. To examine the impact of ethylene conversion on product olefin quality, product olefin content was simulated utilizing 1-butene as a diluent, which is also one of the product olefins produced in the oligomerization reactor, rather than cyclohexane. See entries 3 and 8 of Table 2. Thus, 1208 of 1-butene was introduced into the reactor, followed by catalyst and cocatalyst.
Ethylene was fed to the reactor by demand and the semi-continuous oligomerization experiment was performed at 500 prig of ethylene. In Figs. 9 and 10, conversion, measured as the amount of product olefins foamed, increases as the percentage of butene present decreases. In the single run oligomerization, the mass of the diluent, I-butene, decreases from I00 percent due to ethylene oligomerization to product olefins. Fig. 9 indicates that a high 1-hexene purity was obtained in this run. The lowest r 1-hexane purity point, near 50 mass percent 1-butane, is due to increased paraffin content (0.7 percent vs 0.2 percent for other points) resulting from low ethylene conversion. In Fig. 10, 1-~ctene purity remains over 9~ percent when running the reaction in 1-butane.
As in Fig. 9, the elevated level of paraffin at low conversion artificially lowers the olefin purity. Figs. 9 and 10, which were composed using data from the 500 psig run, may be viewed as extensions of Figs. 6 'and 7, respectively. When using 1-butane as the solvent, the product quality remains high, approaching 99 percent for 1-hexane and exceeding 98.2 percent for 1-octane.
[0065] While the present invention has been illustrated and described above in terms of particular apparatus and methods of use, it is apparent that, having the benefit of the teachings herein, equivalent techniques and ingredients may be substituted for those shown, and other changes can be made within the scope of the present invention as defined by the appended claims.

Claims (76)

1. A method comprising:
contacting an oligomerization catalyst system and a feed comprising olefins;
oligomerizing said feed in at least one continuous reactor; and withdrawing from said at least one continuous reactor an effluent comprising product olefins having at least four carbon atoms;
wherein the oligomerization catalyst system comprises iron or cobalt, or combinations thereof; and wherein oligomerization to product olefins having at least four carbon atoms comprises a single pass conversion of ethylene of at least about 40 weight percent.

2. The method of Claim 1, wherein the single pass conversion of ethylene is at least about 65 weight percent.

3. The method of Claim 1, wherein product olefins having twelve carbon atoms comprise at least about 95 weight percent 1-dodecene.

4. The method of Claim 1, wherein the effluent comprises at least about 40 weight percent product olefins having at least four carbon atoms.

5. The method of Claim 1, wherein said product olefins comprise at least about weight percent linear 1-alkenes.

6. The method of Claim 1, wherein said product olefins comprise at least about weight percent alpha olefins having from about 8 to about 20 carbon atoms.

7. The method of Claim 1, wherein said oligomerization catalyst system comprises a metal alkyl or metal hydride species.

8. The method of Claim 7, wherein said metal alkyl or metal hydride species comprises one or more Lewis acids; a combination of one or more Lewis acids and one or more alkylating agents; one or more alkyl aluminum compounds; one or more alkyl aluminoxanes;
methyl aluminoxane (MAO); modified MAO; tri-alkyl aluminum; diethylaluminum chloride (DEAC); or combinations thereof.

9. The method of Claim 1, wherein said oligomerization catalyst system comprises triethylaluminum (TEA), trimethylaluminum (TMA), tri-isobutyl aluminum (TIBA), tri-butyl aluminum, or combinations thereof.

10. The method of Claim 1, wherein the oligomerization catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure I:

wherein R1, R2, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, an inert functional group, or any two of R1-R3, vicinal to one another, taken together may form a ring;
R4 and R5 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or inert functional group; and R6 and R7 may be identical or different, and are independently aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, optionally substituted aryl group in combination with and ~-coordinated to a metal, optionally substituted aromatic hydrocarbon ring, or optionally substituted polyaromatic hydrocarbon moiety.

11. The method of Claim 1, wherein said oligomerization catalyst system is activated in the absence of ethylene.

12. The method of Claim 10, further comprising selecting R1-R7 such that said metal complex is symmetrical.

13. The method of Claim 10, further comprising selecting R1-R7 such that said metal complex is asymmetrical.

14. The method of Claim 1, wherein said oligomerization catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure II:
wherein R1, R2, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or an inert functional group;
R4 and R5 axe each independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl; and Y is a structural bridge, and W, Y, and Z independently comprise hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl having from about 0 to about 30 carbon atoms.

15. The method of Claim 1, wherein said oligomerization catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure III:
wherein R1-R5 each comprise, independently, hydrogen, optionally substituted hydrocarbyl, an inert functional group, or any two of R1-R3 vicinal to one another taken together may form a ring;
Z1, which is different from Z2, is an aryl or substituted aryl group; and Z2 comprises an aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, or an optionally substituted aryl group in combination with and II-coordinated to a metal.

16. The method of Claim 15, wherein Z2 is an aryl, substituted aryl, optionally substituted aromatic heterocyclic moiety, an optionally substituted polyaromatic heterocyclic moiety, an optionally substituted aliphatic heterocyclic moiety, or an optionally substituted aliphatic heterohydrocarbyl moiety.

17. The method of Claim 1, wherein said oligomerization catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure IV:
wherein A1-A6 each comprise, independently, carbon, nitrogen, oxygen, or sulphur;
A1 may be directly bonded to A5;
R1-R12, R14-R15, and, if present, R13, are each, independently, hydrogen, optionally substituted hydrocarbyl, or an inert functional group;
any two of R1-R15, vicinal to one another, taken together may form a ring; and conditionally, when A1-A5 and A6, if present, are all carbon, said atoms constitute the cyclopentadienyl or aryl part of a II-coordinated metal.

18. The method of Claim 1, wherein said oligomerization catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure VI:
wherein R1-R5 and R7-R9 and R12-R14 are each, independently, hydrogen, substituted hydrocarbyl, an inert functional group, or any two of R1-R3, R7-R9, and R12-R14, vicinal to one another, taken together may form a ring; and R6, R10, R11, and R15 are identical and are selected from fluorine or chlorine.

19. The method of Claim 1, wherein said oligomerization catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure VII:
wherein R1-R5 and R7-R9 and R12-R14 are each, independently, hydrogen, substituted hydrocarbyl, an inert functional group, or any two of R1-R3, R7-R9, and R12-R14, vicinal to one another, taken together may form a ring;
R6 is hydrogen, substituted hydrocarbyl, an inert functional group, ox taken together with R7 or R4 to form a ring;

R10 is hydrogen, substituted hydrocarbyl, an inert functional group, or taken together with R9 or R4 to form a ring; and R11 and R15 are, independently, hydrogen or an inert functional group.

20. The method of Claim 1, wherein said oligomerization catalyst system comprises a selective 1-hexene (S1H) catalyst.

21. The method of Claim 20, wherein said oligomerization catalyst system comprises chromium.

22. The method of Claim 1, wherein said at least one continuous reactor comprises a loop reactor, tubular reactor, continuous stirred tank reactor, or combinations thereof.

23. The method of Claim 1, wherein said at least one continuous reactor comprises a loop reactor and fluid flow in said loop reactor comprises a Reynolds number of from about 200,000 to about 700,000.

24. The method of Claim 1, wherein said at least one continuous reactor comprises a tubular reactor and fluid flow in said tubular reactor comprises a Reynolds number of from about 300,000 to about 2,000,000.

25. The method of Claim 1, wherein at steady state the contents of said reactor are not turbid.

26. The method of Claim 1, wherein the effluent comprises a diluent and wherein said diluent comprising aliphatics, non-aliphatics, aromatics, saturated compounds having from .4 to 8 carbon atoms, or combinations thereof.

27. The method of Claim 1, wherein the effluent comprises a diluent and wherein said diluent comprises an aromatic compound having from about 6 to about 30 carbon atoms, or combinations thereof.

28. The method of Claim 1, wherein the effluent comprises a diluent and wherein said diluent comprises cyclohexane, benzene, toluene, xylene, ethylbenzene, or combinations thereof.

29. The method of Claim 1, wherein the effluent comprises a diluent and wherein said diluent comprises olefins having from about 4 to about 30 carbon atoms, or combinations thereof.

30. The method of Claim 1, wherein the effluent comprises a diluent and wherein said diluent comprises 1-butene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1-octadecene, or combinations thereof.

31. The method of Claim 1, further comprising manipulating product olefin distribution by modifying a pressure of the reactor.

32. The method of Claim 1, further comprising injecting said feed and said catalyst system into said reactor at more than one point along the length of said reactor wherein said reactor is a tubular reactor.

33. The method of Claim 1, further comprising cooling said reactor with a coolant more volatile than water.

34. The method of Claim 1, further comprising cooling said reactor with a coolant, wherein said coolant comprises butane, isobutane, isopentane, or combinations thereof.

35. The method of Claim 1, wherein said reactor comprises a temperature of from about 40 to about 150 degrees Celsius.

36. A method comprising:
contacting an oligomerization catalyst system and a feed comprising olefins;
oligomerizing said feed in at least one continuous reactor; and withdrawing from said at least one continuous reactor an effluent comprising product olefins having at least four carbon atoms;

wherein oligomerization to product olefins having at least four carbon atoms comprises a single pass conversion of ethylene of at least about 65 weight percent; and wherein product olefins having twelve carbon atoms comprise at least about 95 weight percent 1-dodecene.

37. The method of Claim 36, wherein the catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure I:
wherein R1, R2, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, an inert functional group, or any two of R1-R3, vicinal to one another, taken together may form a ring;
R4 and R5 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or inert functional group; and R6 and R7 may be identical or different, and are independently aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, optionally substituted aryl group in combination with and II-coordinated to a metal, optionally substituted aromatic hydrocarbon ring, or optionally substituted polyaromatic hydrocarbon moiety.

38. The method of Claim 37, further comprising selecting R1-R7 such that said metal complex is symmetrical.

39. The method of Claim 37, further comprising selecting R1-R7 such that said metal complex is asymmetrical.

40. The method of Claim 36, wherein the catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure II:
wherein R1, R2, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or an inert functional group;
R4 and R5 are each independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl; and Y is a structural bridge, and W, Y, and Z independently comprise hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl having from about 0 to about 30 carbon atoms.

41. The method of Claim 36, wherein the catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure III:
.xi.

wherein R1-R5 each comprise, independently, hydrogen, optionally substituted hydrocarbyl, an inert functional group, or any two of Rl-R3 vicinal to one another taken together may form a ring;
Zl, which is different from Z2, is an aryl or substituted aryl group; and Z2 comprises an aryl, substituted aryl, optionally substituted heterohydrocarbyl moiety, or an optionally substituted aryl group in combination with and II-coordinated to a metal.

42. The method of Claim 41, wherein Z2 is an aryl, substituted aryl, optionally substituted aromatic heterocyclic moiety, an optionally substituted polyaromatic heterocyclic moiety, an optionally substituted aliphatic heterocyclic moiety, or an optionally substituted aliphatic heterohydrocarbyl moiety.

43. The method of Claim 36, wherein the catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure IV:

wherein Al-A6 each comprise, independently, carbon, nitrogen, oxygen, or sulphur;
A1 may be directly bonded to A5;
Rl-R12, R14-R15, and, if present, R13, are each, independently, hydrogen, optionally substituted hydrocarbyl, or an inert functional group;
any two of Rl-Rl5, vicinal to one another, taken together may form a ring; and conditionally, when Al-A5 and A6, if present, are all carbon, said atoms constitute the cyclopentadienyl or aryl part of a II-coordinated metal.

44. The method of Claim 36, wherein the catalyst system comprises a metal complex activated by a co-catalyst and wherein said metal complex comprises a ligand having chemical structure VI:
wherein R1-R5 and R7-R9 and R12-R14 are each, independently, hydrogen, substituted hydrocarbyl, an inert functional group, or any two of Rl-R3, R7-R9, and R12-R14, vicinal to one another, taken together may form a ring; and R6, Rl0, R11 and R15 are identical and are selected from fluorine or chlorine.

45. The method of Claim 36, wherein the catalyst system comprises a metal complex activated by a co-catalyst and wherein. said metal complex comprises a ligand having chemical structure VII:

wherein Rl-R5 and R7-R9 and R12-Rl4 are each, independently, hydrogen, substituted hydrocarbyl, an inert functional group, or any two of Rl-R3, R7-R9, and Rl2-Ri4, vicinal to one another, taken together may form a ring;
R6 is hydrogen, substituted hydrocarbyl, an inert functional group, or taken together with R7 or R4 to form a ring;
Rl0 is hydrogen, substituted hydrocarbyl, an inert functional group, or taken together with R9 or R4 to form a ring; and Rll and R15 are, independently, hydrogen or an inert functional group.

46. The method of Claim 36, wherein the effluent comprises at least about 40 weight percent product olefins having at least four carbon atoms.

47. The method of Claim 36, wherein said product olefins comprise at least about 80 weight percent linear 1-alkenes.

48. The method of Claim 36, wherein said product olefins comprise at least about 20 weight percent alpha olefins having from about 8 to about 20 carbon atoms.

49. The method of Claim 36, wherein said oligomerization catalyst system comprises a metal alkyl or metal hydride species.

50. The method of Claim 49, wherein said metal alkyl or metal hydride species comprises one or more Lewis acids; a combination of one or more Lewis acids and one or more alkylating agents; one or more alkyl aluminum compounds; one or more alkyl aluminoxanes;
methyl aluminoxane (MAO); modified MAO; tri-alkyl aluminum; diethylaluminum chloride (DEAC); or combinations thereof.

51. The method of Claim 36, wherein said oligomerization catalyst system comprises triethylaluminum (TEA), trimethylaluminum (TMA), Tri-isobutyl Aluminum (TIBA), Tri-butyl Aluminum, or combinations thereof.

52. The method of Claim 36, wherein the effluent comprises a diluent and wherein said diluent comprises an aromatic compound having from about 6 to about 30 carbon atoms, or combinations thereof.

53. The method of Claim 36, wherein the effluent comprises a diluent and wherein said diluent comprises cyclohexane, benzene, toluene, xylene, ethylbenzene, or combinations thereof.

54. The method of Claim 36, wherein the effluent comprises a diluent and wherein said diluent comprises olefins having from about 4 to about 30 carbon atoms, or combinations thereof.

55. The method of Claim 36, wherein the effluent comprises a diluent and wherein said diluent comprises 1-butene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1-octadecene, or combinations thereof.

56. The method of Claim 36, further comprising manipulating product olefin distribution by modifying a pressure of the reactor.

57. The method of Claim 36, further comprising injecting said feed and said catalyst system into said reactor at more than one point along the length of said reactor wherein said reactor is a tubular reactor.

58. The method of Claim 36, further comprising cooling said reactor with a coolant more volatile than water.

59. The method of Claim 36, further comprising cooling said reactor with a coolant, wherein said coolant comprises butane, isobutane, isopentane, or combinations thereof.

60. The method of Claim 36, wherein said reactor comprises a temperature of from about 40 to about 150 degrees Celsius.

61. The method of Claim 36, wherein said catalyst system comprises a transition metal.

62. The method of Claim 36, wherein said catalyst system comprises iron or cobalt, or combinations thereof.

63. The method of Claim 36, wherein said catalyst system comprises nickel.

64. The method of Claim 36, wherein said reactor comprises a loop reactor, tubular reactor, continuous stirred tank reactor, or combinations thereof.

65. The method of Claim 36, wherein said at least one continuous reactor comprises a loop reactor and fluid flow in said loop reactor comprises a Reynolds number of from about 200,000 to about 700,000.

66. The method of Claim 36, wherein said at least one continuous reactor comprises a tubular reactor and fluid flow in said tubular reactor comprises a Reynolds number of from about 300,000 to about 2,000,000.

67. The method of Claim 36, wherein at steady state the contents of said reactor are not turbid.

68. A method of oligomerizing alpha olefins comprising contacting a metal complex having chemical structure VIII with a co-catalyst and a feed comprising olefins:
~
wherein R1, R2, and R3 are each independently hydrogen, hydrocarbyl, substituted hydrocarbyl, or an inert functional group;
R4 and R5 are each independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl;

Y is a structural bridge, and W, Y, and Z are independently hydrogen, hydrocarbyl, an inert functional group, or substituted hydrocarbyl having from about 0 to about 30 carbon atoms;
wherein Ml and M2 are metal atoms that are independently selected from a group comprising cobalt, iron, chromium, and vanadium;
each X is an anion; and n is 1, 2, or 3, so that the total number of negative charges on X is equal to the oxidation state of Ml or M2 .

69. The method of Claim 68, further comprising:
withdrawing from a continuous reactor an effluent comprising at least about 25 weight percent product olefins having at least four carbon atoms.

70. The method of Claim 68, further comprising:
withdrawing from a continuous reactor an effluent comprising at least about 40 weight percent product olefins having at least four carbon atoms.

71. The method of Claim 68, further comprising:
withdrawing from a continuous reactor an effluent comprising product olefins having twelve carbon atoms wherein said product olefins having twelve carbon atoms comprise at least about 95 weight percent 1-dodecene.

72. The method of Claim 68, further comprising:
withdrawing product olefins from a continuous reactor wherein said product olefins comprise at least about 20 weight percent alpha olefins having from about 8 to about 20 carbon atoms.

73. The method of Claim 68, further comprising:
withdrawing product olefins from a continuous reactor wherein said product olefins comprise from about 20 to about 80 weight percent olefins having 6 carbon atoms and wherein said product olefins comprise at least about 20 weight percent olefins having greater than 6 carbon atoms.

74. The method of Claim 68, further comprising:
withdrawing from a continuous reactor product olefins comprising olefins having six carbon atoms wherein said olefins having six carbon atoms comprise at least about 98 weight percent 1-hexene.

75. An alpha olefin prepared according to the method of claim 1.

76. An alpha olefin prepared according to the method of claim 36.