LINEAR ALPHA OLEFIN PRODUCTION USING A TANK GROWTH REACTOR

Abstract: A method for preparing C₄ to C₁₀ α-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 α-olefins at 100-150°C, 1.5-13.9 MPa, and 5-90 minute contact time followed by displacement with lower α-olefins in a static mixer zone to free the growth α-­ olefins and regenerate the trialkyl aluminum compounds. The growth α-olefins are separated with all of the lower α--­ olefins recycled to the growth and displacement steps.

Description: LINEAR ALPHA OLEFIN PRODUCTION USING A TANK GROWTH REACTOR The production of alpha olefins having unbranched carbon skeletal configurations and terminal unsaturation has been practiced for many years. 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 C12 to C18 a-olefins for detergent use and the C1O+ for synthetic lubricants. The lower carbon atom compounds, viz. C6 to C8 have recently found utility in the polymer field and thus are being recovered in increasing volume. In U.S. Patent 4,314,090, there is disclosed a process which provides for the producton of increased amounts of C4-C1O alpha olefins using an elongated coil growth reactor such as well known from U.S. 2,971,969. 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-l and octene-l 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. Preferably, the growth promoting conditions used in the tank reactor are a temperature of 100 to 1500C and preferably 115 to 1250C, a pressure range from 1.5-13.9 MPa and preferably 2.2-10.5 MPa and a liquid residence time of 15 to 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 and 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 ofthe 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. The invention is further illustrated by the Figure of the attached drawing. In the drawing, 10 is a feed line supplying ethylene, propylene, or butene-l, and preferable ethy lene 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 4.9 MPa. 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 a-olefins of C4 -C2 o 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 a-olefins (C6-C1O) 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 C12 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 a-olefins. In accordance with the present invention, â lower olefin such as ethylene after being pressurized to a range from 2.2-7.0 MPa is fed to a tank reactor maintained at a pressure of from 1.5-13.9 MPa and preferably from 2.2-10.5 MPa and a temperature of 1000C to 1500C and preferably from 1150C to 1250C 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 5 and 90 minutes and preferably from 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 a-olefin of 2-4 carbon atoms or preferably a mixture of ethylene and butene-l 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 2000C to 3500C and preferably in the range from 2500C to 2800C. The reactor pressure is maintained at 0.1-7.0 MPa and preferably in the range from 0.79-1.48 MPa. 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 1500C 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 C4 to C10 a-olefins, which may be further separated in its constituent components. The third separator strips any remaining a-olefins from the tri lower alkyl aluminum growth material which olefins are combined with the a-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-C14) 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 4.9 MPa. The reactor was brought to a 1260C operating temperature via electric tape heaters. The pump was started and set to flow 50 cc/min. of liquid. This represents a 1 1/2 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-l 22.0% wt. Hexene-l 58.7% wt. Octene-l 16.6% wt. Decene-l 2.6% wt. C12+ 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-C14 76.0 gms The solution recycle rate was set at 50 cc/min. with the reactor operating at 4.9 MPa and 1130C. 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-l 8.9% wt. Hexene-l 61.3% wt. Octene-l 23.7% wt. Decene-1 5.8% wt. C12+ 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-C14) 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 4.9 MPa and 1170C for 20 minutes residence time. The following yields were noted: Butene-l 18.9% wt. Hexene-l 66.9% wt. Octene-l 13.0% wt. C12+ 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-C14 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 4.9 MPa and 1200C for 30 minutes residence time. The following yields were noted: Butene-l 19.6% wt. Hexene-l 57.4% wt. 'Octene-l. 18.5% wt. Decene-l 4.0% wt. C12+ 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-C14 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 3.6 MPa and 1200C for 30 minutes residence time. The following yields were noted: Butene-l 22.2% wt. Hexene-l 57.6% wt. Octene-l 16.2% wt. Decene-l 3.5% wt. C12+ 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-C14 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 4.9 MPa and llO"C for 30 minutes residence time. The following yields were noted: Butene-l 22.23% wt. Hexene-l 60.11% wt. Octene-l 15.0% wt. Decene-l 2.34% wt. C12+ 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-C14 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 4.9 MPa and 1150C for 30 minutes residence time. The following yields were noted: Butene-1 16.9% wt. Hexene-l 60.8% wt. Octene-l 17.6% wt. Decene-l 3.9% wt. C12+ 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-C14 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 4.9 MPa and 1130C for 30 minutes residence time. The following yields were noted: Butene-l 8.8% wt. Hexene-l 61.3% wt. Octene-l 23.6% wt. Decene-l 5.8% wt. C12+ 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-C14 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 6.3 MPa and 1210C for 30 minutes residence time. The following yields were noted: Butene-l 4.3% wt. Hexene-l 56.2% wt. Octene-l 26.7% wt. Decene-l 9.8% wt. C12+ 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-C14 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 4.9 MPa and 1300C for 15 minutes residence time. The following yields were noted: Butene-l 24.2% wt. Hexene-1 55.3% wt. Octene-l 16.4% wt. Decene-l 3.5% wt. C12+ 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-C14 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 4.9 MPa and 1300C for 30 minutes residence time. The following yields were noted: Butene-l 21.2% wt. Hexene-l 53.2% wt. Octene-l 19.8% wt. Decene-l 5.0% wt. C12+ 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-C14 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 2.2 MPa and 1200C for 30 minutes residence time. The following yields were noted: Butene-l 19.7% wt. Hexene-l 75.4% wt. Octene-l 4.9% wt. Decene-l 0.0% wt. C12+ 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-C14 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 10.5 MPa and 1200C for 30 minutes residence time. The following yields were noted: Butene-1 13.3% wt. Hexene-l 58.14% wt. Octene-l 22.43% wt. Decene-l 5.4% wt. C12+ 0.73% wt.

Claims: CLAIMS 1. In a process for making C4-Ct a-olefins wherein an a-olefin having 2-4 carbon atoms or mixtures thereof and low molecular weight trialkyl aluminum are reacted in a growth reaction zone under growth promoting conditions to provide higher molecular weight trialkyl aluminum and reacting an a-olefin having 2-4 carbon atoms or mixtures thereof with said higher trialkyl aluminum in a displacement reactor zone under displacement conditions to provide a mixture of C4 -C10 a-olefins, the improvement which comprises providing a growth reaction zone by reacting 2 to 6 moles of a-olefin per mole of trialkyl aluminum in a tank reaction zone and having a recirculation rate through an external heat transfer zone such that the reaction zone contents are completely recirculated in a period of time sufficient to remove the heat of said reaction zone and maintain a substantially constant temperature therein. 2. The process as set forth in Claim 1 wherein the recirculation time is 0.1 to 30.0 minutes. 3. The process as set forth in Claim 2 wherein the recirculation time is 0.5 to 3.0 minutes. 4. The process as set forth in Claim 1, 2 or 3 wherein the growth promoting conditions are a temperature of 100 to 1400C, a pressure of 1.5 to 13.9 MPa, and a liquid residence time from 15 to 45 minutes. 5. The process as set forth in Claim 4 wherein the growth promoting conditions are a temperature of 115 to 1250C, a pressure of 2.2 to 10.5 MPa, and a liquid residence time from 30 to 40 minutes. 6. A process for making C4 -C10 a-olefins which comprises A) reacting 2 to 6 moles of an a-olefin having 2-4 carbon atoms or mixtures thereof per mol of trialkyl aluminum in a tank reaction zone under a pressure of 1.5 to 13.9 MPa and a temperature in the range from 1000C to 1500C wherein said zone has a recirculation rate through an external heat transfer zone such that the contents thereof are recirculated in a period of time sufficient to remove the heat of said reaction zone so as to maintain a substantially constant tem perature therein and to provide a growth product comprising higher trialkyl aluminum, B) reacting an a-olefin having 2-4 carbon atoms, or mixtures thereof with said growth product in a displacement zone having a temperature in the range from 2000C to 3500C, a pressure in the range from 0.1 to 7.0 MPa and a contact time in the range from 0.1 to 5 seconds, and C) recovering the C4-C,o a-olefins. 7. A process for making C4 -C10 a-olefins which comprises A) reacting 2 to 6 moles of ethylene per mol of trialkyl aluminum in a tank reaction zone under a pressure of 1.5-13.9 MPa and a temperature in the range from 1000C to 15O0C wherein said zone has a recirculation rate through an external heat transfer zone such that the contents thereof are recirculated in a period of time from 0.5 to 3 minutes to provide a growth product comprising higher trialkyl aluminum, B) reacting ethylene or butene-l or mixtures thereof with said growth product in a displacement zone having a temperature in the range from 2000C to 3500C, a pressure in the range from 0.1 to 7.0 MPa and a contact time in the range from 0.1 to 5 seconds, and C) recovering the C4-C,o a-olefins. 8. The process as set forth in any preceding Claim wherein said displacement zone comprises a static mixer zone. 9. The process as set forth in Claim 8 wherein said static mixer zone has 3 to 30 fixed elements. 10. The process as set forth in Claim 7 wherein the tank reaction zone is under a pressure of 2.2 to 10.5 MPa and has a temperature in the range from 1150 to 1250C and the displacement zone is under a pressure of 0.8 to 1.5 MPa and has a temperature in the range from 2500 to 2800C.

Inventors: FOWLER, ALLAN EUGENE, SIMS, STEVE AUSTIN, WHITE, GORDON ELDON
Applicants: THE DOW CHEMICAL COMPANY
Application year: 1982
Main classification: C07C2
IPC codes: C07C2