Linear alpha olefin production using a tank growth reactor

A method for preparing C.sub.4 to C.sub.10 .alpha.-olefins employing trialkyl aluminum compounds, in a growth zone having a recirculation rate through an external heat transfer zone such that the contents of the zone are recirculated in a period of time sufficient to remove the heat of the reaction using added lower .alpha.-olefins at 100.degree.-150.degree. C., 200-2000 psig, and 5-90 minute contact time followed by displacement with lower .alpha.-olefins in a static mixer zone to free the growth .alpha.-olefins and regenerate the trialkyl aluminum compounds. The growth .alpha.-olefins are separated with all of the lower .alpha.-olefins recycled to the growth and displacement steps.

BACKGROUND OF THE INVENTION 
The production of alpha olefins having unbranched carbon skeletal 
configurations and terminal unsaturation has been practiced for 20 or more 
years. See for example, Chemical Engineering Progress 58:85-90 (June 1962) 
and U.S. Pat. No. 3,227,773, dated Jan. 4, 1966. With the advent of the 
triorganometallic compounds, viz, triethyl and tri-n-butyl aluminum, large 
scale commercial production has occurred. The primary and desired products 
are the C.sub.12 to C.sub.18 .alpha.-olefins for detergent use and the 
C.sub.10.sbsb.+ for synthetic lubricants. The lower carbon atom compounds, 
viz, C.sub.6 to C.sub.8 have recently found utility in the polymer field 
and thus they are being recovered from the present day processes in 
increasing volume. In Ser. No. 179,348 filed Aug. 18, 1980, there is 
disclosed a process which provides for the production of increased amounts 
of C.sub.4 -C.sub.10 alpha olefins. 
The use of elongated coil growth reactors is well known from U.S. Pat. No. 
2,971,969. 
SUMMARY OF THE INVENTION 
It is known to use coil reactors to perform the growth reaction step. 
However, these reactors require an olefin:aluminum alkyl ratio of about 10 
to 1 for best results. It has been found that by using a tank reactor with 
a relatively rapid external recirculation rate it is possible to use 2 to 
6 moles of olefin per mole of aluminum alkyl and achieve yields of the 
desired hexene-1 and octene-1 after the displacement reaction which is as 
high as the system using coil reactors. 
An added advantage of the present invention is the reduction in the amount 
of energy and capital equipment costs required by using the lower ratios 
of olefin. In fact, no excess olefin is required thereby eliminating 
costly recycle compression. 
The growth promoting conditions used in the tank reactor are a temperature 
of 100.degree. to 150.degree. C. and preferably 115.degree. to 125.degree. 
C., a pressure range from 200 to 2000 pounds per square inch and 
preferably 300 to 1500 psig, and a liquid residence time of 15-60 minutes 
and preferably 30 to 40 minutes. 
The growth reaction zone contents are recirculated through an external heat 
transfer zone at a recirculation rate such that the reaction zone contents 
are completely recirculated for a time sufficient to remove the heat of 
the reaction so as to maintain a substantially constant temperature. 
Preferably the recirculation time period is 0.1 to 30.0 minutes and 0.5 to 
3.0 minutes is the most preferred time period. 
A further aspect of the present invention is the use of a displacement zone 
containing a static mixer having 3 to 30 fixed elements which speeds up 
the displacement reaction.

In the drawing, 10 is a feed line supplying ethylene, propylene, or 
butene-1, and preferable ethylene which has been suitably purified to 
remove moisture and oxygen. Item 12 is a compressor wherein the lower 
olefin feed is brought up to a pressure of about 700 psig. The compressed 
olefin is then fed by line 14 to line 16 where it is combined with 
recycled catalyst from line 18 and circulated through the heat exchanger 
17, the pump 19 and the recycle line 21 to the reactor inlet 22. 
The pressurized tank or growth reactor 20 is provided with a gaseous outlet 
23 for unreacted gases which circulate via line 25 through a heat 
exchanger 26 and line 28 to the displacement feed line 30. The combined 
liquid feed from line 30 and the gas feed from line 28 are thus combined 
to provide a feed to the displacement reactor 32. Reduction valves 24 and 
27 are provided to maintain the high pressure in the reactor 20. 
In the displacement reactor 32, liquid growth material is reacted with the 
displacement gases to generate growth .alpha.-olefins of C.sub.4 -C.sub.20 
and also recover the organo metallic catalyst. The reactor 32 is a 
conventional static mixer. 
The contents of the displacement reactor 32 are fed by line 34 into the 
extraction column 36 wherein lower olefins or ethylene is stripped from 
the reaction mixture and is removed by outlet 42, and line 48. A recycle 
line 46, condenser 44 and a recycle inlet 40 is provided to remove the 
heavier gases and return them as liquid reflux. The line 48 carries the 
lower olefins to a compressor 50 where the gases are brought back up to 
the proper pressure for introduction by line 52 into the recycle line 28. 
The bottoms from the tower 36 are removed by outlet 38 and introduced by 
line 39 into the tower 54 by inlet 53. In a manner similar to the tower 
36, a higher olefin such as butene gas is stripped via the outlet 64, 
condenser 66 and inlet 62, with line 68 removing the butene gas to a 
takeoff valve 70 and transfer line 72. If desired, some or most of the 
butene can be withdrawn from valve 70 for use as an intermediate. The 
remaining butene is thus recycled by line 72 back to line 48 for reuse as 
a displacing gas. 
The liquid bottoms in the butene tower 54 are recirculated via outlet 56, 
re-boiler 58, and inlet 60. The bottoms are fed by line 59 to inlet 74 of 
the vacuum tower 76 wherein the desired .alpha.-olefins (C.sub.6 
-C.sub.10) are separated from the catalyst mixture. The vacuum tower 76 is 
provided with a vacuum line 98 for the necessary reduction in pressure. 
The bottoms from the vacuum tower 76 are drawn off by outlet 84 and 
circulated by pump 82 through a re-boiler 80 and back to the tower 76 by 
inlet 78. 
A portion of the vacuum tower bottoms are recycled by line 86 back to the 
growth reactor 20. A reflux circuit for the vacuum tower 76 is provided by 
line 90, condenser 92 and inlet 94. A purge line 57 is provided to 
periodically remove C.sub.12 and higher molecular weight material. 
The vacuum tower overhead products are removed by outlet 88 and sent to a 
heat exchanger 96 and removed for further separation into the desired 
.alpha.-olefins. 
DETAILED DESCRIPTION OF THE INVENTION 
In accordance with the present invention, a lower olefin such as ethylene 
after being pressurized to a range from about 300 to 1000 psig is fed to a 
tank reactor maintained at a pressure of from about 200 to about 2000 psig 
and preferably from about 300 to about 1500 psig and a temperature of 
about 100.degree. C. to about 150.degree. C. and preferably from about 
115.degree. C. to about 125.degree. C. wherein the olefin reacts with a 
trialkyl aluminum growth material, viz. triethyl aluminum or tributyl 
aluminum and preferably a mixture of the two, high in triethyl aluminum 
content. The reactor is of such size to enable the reactants to be in 
contact between about 5 and 90 minutes and preferably from about 30 to 40 
minutes. Due to the exothermic reaction, the pressurized tank reactor is 
provided with an external heat transfer device so that the reaction zone 
contents are completely recirculated in a period of time from 0.25 to 5 
minutes and preferably 0.5 to 3 minutes. Product withdrawn from the growth 
reactor is cooled to insure the growth products and any unreacted growth 
material remain in the liquid state yet the olefin or ethylene which has 
not reacted can be separated and returned to the growth reactor as recycle 
olefin. 
The cooled liquid growth product and any unreacted growth material is then 
mixed with a displacement gas, such as .alpha.-olefin of 2-4 carbon atoms 
or preferably a mixture of ethylene and butene-1 in a static mixer 
displacement reactor of such size as to displace the material fed in under 
six seconds. The displacement gas is preheated to a temperature such that 
when mixed with the liquid feed stream at the displacement reactor, the 
temperature will be in the range from 200.degree. C. to 350.degree. C. and 
preferably in the range from 250.degree. C. to 280.degree. C. The reactor 
pressure is maintained at about 0-1000 psig and preferably in the range 
from 100 to 200 psig. The static mixer has 3 to 30 elements and preferably 
6 to 12 elements so that a relatively short contact time in the range from 
0.1 to 5 seconds, and is preferably in the range from 0.5 to 1.0 seconds, 
is achieved with complete mixing of the gas and liquid. The mol ratio of 
the displacement gas to each alkyl group of the trialkyl aluminum is in 
the range from 10:1 to 50:1 and preferably in the range 25:1 to 30:1. 
The displacement product, the olefins and the tri lower alkyl aluminum 
product, is rapidly cooled to below about 150.degree. C. and fed to the 
first stage of a separator 36 wherein the displacement gas and the olefins 
are removed and sent to a second stage separator 54 and the liquid product 
remaining is directed to a third stage separator 76. The gaseous products 
delivered to the second stage separator are further cooled and the 
displacement gases, removed, recompressed, heated, and recycled to the 
displacement reactor feed stream. The liquid bottoms product from the 
second separation is the desired olefins, in this case C.sub.4 to C.sub.10 
.alpha.-olefins, which may be further separated in its constituent 
components. The third separator strips any remaining .alpha.-olefins from 
the tri lower alkyl aluminum growth material which olefins are combined 
with the .alpha.-olefins from the second separator and the latter, the 
lower alkyl aluminum compounds are recycled to the growth reactor. 
Illustrative of the effectiveness of the tank reaction zone with 
recirculation, the conditions and results of thirteen typical examples are 
shown below wherein all percentages are in weight percent. 
EXAMPLE 1 
A 250 cc tank reactor was charged with the following materials: 
______________________________________ 
triethyl aluminum (TEA) 17.07 gms 
tri-n-butyl aluminum (TNBA) 
11.38 gms 
tetradecane (n - C.sub.14) 
28.45 gms 
______________________________________ 
This represents a 50% by weight aluminum alkyl feed stream. 
The reactor had a bottom outlet connected to a recycle pump which pumped 
the reactor contents through a cooling coil back into the reactor. 
A total of 31.8 grams of ethylene gas was charged at 700 psig. The reactor 
was brought to a 126.degree. C. operating temperature via electric tape 
heaters. The pump was started and set to flow 50 cc/min. of liquid. This 
represents a 11/2 minute reactor volume turnover. 
The reaction was allowed to run for 30 minutes and then cooled down to room 
temperature. The aluminum alkyls were collected and a material balance was 
done. The aluminum alkyls, when slowly hydrolyzed, showed the following 
olefin yields: 
______________________________________ 
Butene-1 22.0% wt. 
Hexene-1 58.7% wt. 
Octene-1 16.6% wt. 
Decene-1 2.6% wt. 
C.sub.12.sbsb.+ 0.1% wt. 
Total 100.0% wt. 
______________________________________ 
EXAMPLE 2 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 11.4 gms 
TNBA 7.6 gms 
n - C.sub.14 76.0 gms 
______________________________________ 
The solution recycle rate was set at 50 cc/min. with the reactor operating 
at 700 psig and 113.degree. C. A total of 35.3 grams of ethylene was 
charged to the reactor during the reactor operation. 
After 30 minutes residence time, the following yields were noted: 
______________________________________ 
Butene-1 8.9% wt. 
Hexene-1 61.3% wt. 
Octene-1 23.7% wt. 
Decene-1 5.8% wt. 
C.sub.12.sbsb.+ 0.3% wt. 
______________________________________ 
EXAMPLE 3 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
triethyl aluminum (TEA) 28.5 grams 
tri n-butyl aluminum (TNBA) 
19.0 grams 
tetradecene (n - C.sub.14) 
47.5 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 2.5 
minute reactor volume turnover. A total 27.8 grams ethylene gas was 
charged with the reactor operating at 700 psig and 117.degree. C. for 20 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 18.9% wt. 
Hexene-1 66.9% wt. 
Octene-1 13.0% wt. 
Decene-1 1.2% wt. 
C.sub.12.sbsb.+ 0.0% wt. 
______________________________________ 
EXAMPLE 4 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 16.9 grams 
TNBA 11.3 grams 
n - C.sub.14 28.2 grams 
______________________________________ 
The solution recycle rate was set at 75 cc/min. This represents a 1.0 
minute reactor volume turnover. A total 32.2 grams ethylene gas was 
charged with the reactor operating at 700 psig and 120.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 19.6% wt. 
Hexene-1 57.4% wt. 
Octene-1 18.5% wt. 
Decene-1 4.0% wt. 
C.sub.12.sbsb.+ 0.5 wt. 
______________________________________ 
EXAMPLE 5 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 17.0 grams 
TNBA 11.3 grams 
n - C.sub.14 28.4 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 1.5 
minute reactor volume turnover. A total 19.8 grams ethylene gas was 
charged with the reactor operating at 500 psig and 120.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 22.2% wt. 
Hexene-1 57.6% wt. 
Octene-1 16.2% wt. 
Decene-1 3.5% wt. 
C.sub.12.sbsb.+ 0.5% wt. 
______________________________________ 
EXAMPLE 6 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 16.8 grams 
TNBA 11.2 grams 
n - C.sub.14 28.0 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 1.5 
minute reactor volume turnover. A total 29.8 grams ethylene gas was 
charged with the reactor operating at 700 psig and 110.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 22.23% wt. 
Hexene-1 60.11% wt. 
Octene-1 15.0% wt. 
Decene-1 2.34% wt. 
C.sub.12.sbsb.+ 0.32% wt. 
______________________________________ 
EXAMPLE 7 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 5.7 grams 
TNBA 3.8 grams 
n - C.sub.14 85.3 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 2.5 
minute reactor volume turnover. A total 31.5 grams ethylene gas was 
charged with the reactor operating at 700 psig and 115.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 16.9% wt. 
Hexene-1 60.8% wt. 
Octene-1 17.6% wt. 
Decene-1 3.9% wt. 
C.sub.12.sbsb.+ 0.8% wt. 
______________________________________ 
EXAMPLE 8 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 11.4 grams 
TNBA 7.6 grams 
n - C.sub.14 76.0 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 2.5 
minute reactor volume turnover. A total 35.3 grams ethylene gas was 
charged with the reactor operating at 700 psig and 113.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 8.8% wt. 
Hexene-1 61.3% wt. 
Octene-1 23.6% wt. 
Decene-1 5.8% wt. 
C.sub.12.sbsb.+ 0.5% wt. 
______________________________________ 
EXAMPLE 9 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 17.0 grams 
TNBA 11.3 grams 
n - C.sub.14 28.4 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 1.5 
minute reactor volume turnover. A total 39.0 grams ethylene gas was 
charged with the reactor operating at 900 psig and 121.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 4.3% wt. 
Hexene-1 56.2% wt. 
Octene-1 26.7% wt. 
Decene-1 9.8% wt. 
C.sub.12.sbsb.+ 3.0% wt. 
______________________________________ 
EXAMPLE 10 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 22.68 grams 
TNBA 15.12 grams 
n - C.sub.14 37.80 grams 
______________________________________ 
The solution recycle rate was set at 67 cc/min. This represents a 1.5 
minute reactor volume turnover. A total of 45.3 grams ethylene gas was 
charged with the reactor operating at 700 psig and 130.degree. for 15 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 24.2% wt. 
Hexene-1 55.3% wt. 
Octene-1 16.4% wt. 
Decene-1 3.5% wt. 
C.sub.12.sbsb.+ 0.6% wt. 
______________________________________ 
EXAMPLE 11 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 22.68 grams 
TNBA 15.12 grams 
n - C.sub.14 37.80 grams 
______________________________________ 
The solution recycle rate was set at 67 cc/min. This represents a 1.5 
minute reactor volume turnover. A total of 45.3 grams ethylene gas was 
charged with the reactor operating at 700 psig and 130.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 21.2% wt. 
Hexene-1 53.2% wt. 
Octene-1 19.8% wt. 
Decene-1 5.0% wt. 
C.sub.12.sbsb.+ 0.9% wt. 
______________________________________ 
EXAMPLE 12 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 17.04 grams 
TNBA 11.36 grams 
n - C.sub.14 28.40 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 1.5 
minute reactor volume turnover. A total of 12.5 grams ethylene gas was 
charged with the reactor operating at 300 psig and 120.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 19.7% wt. 
Hexene-1 75.4% wt. 
Octene-1 4.9% wt. 
Decene-1 0.0% wt. 
C.sub.12.sbsb.+ 0.0% wt. 
______________________________________ 
EXAMPLE 13 
Using the same reactor set up as Example No. 1, the following conditions 
were noted: 
______________________________________ 
Charge 
______________________________________ 
TEA 17.07 grams 
TNBA 11.38 grams 
n - C.sub.14 28.45 grams 
______________________________________ 
The solution recycle rate was set at 50 cc/min. This represents a 1.5 
minute reactor volume turnover. A total of 67.2 grams ethylene gas was 
charged with the reactor operating at 1500 psig and 120.degree. C. for 30 
minutes residence time. 
The following yields were noted: 
______________________________________ 
Butene-1 13.3% wt. 
Hexene-1 58.14% wt. 
Octene-1 22.43% wt. 
Decene-1 5.4% wt. 
C.sub.12.sbsb.+ 0.73% wt. 
______________________________________