TWI544962B - Catalyst composition for oligomerization of ethylene - Google Patents

Description

Catalyst composition for oligoethylene

The present invention relates to a catalyst composition for oligoethylene, a method for producing a linear alpha-olefin by oligoethylene, and a method for preparing a catalyst composition.

Linear alpha-olefins having from 4 to 20 carbon atoms are key raw materials in the manufacture of surfactants, plasticizers, synthetic lubricants and polyolefins. High purity alpha-olefins are particularly valuable in the manufacture of low density polyethylene and in oxo (oxo) processes. Linear alpha-olefins are more reactive than branched chain alpha-olefins; the branching of alpha-carbons dramatically reduces reactivity. In this regard, linear alpha-olefins having 6 to 18 carbon atoms, especially having 6 to 10 carbon atoms, are particularly useful and are widely used in large quantities.

Although the linear olefin is a dehydrogenation product of a linear alkane, a major portion of such a product is composed of internal olefins. The preparation of alpha-olefins is based primarily on the oligomerization of ethylene.

These linear alpha olefins are typically prepared by catalytic oligomerization of ethylene in the presence of a Ziegler type catalyst. The key to ethylene oligomerization is to achieve the desired selectivity and product distribution. Catalyst and process conditions play an important role in this category.

Catalysts for oligomerizing ethylene into linear C ₄ -C ₃₀ α-olefins are known to include zirconium tetrachloride and organoaluminum compounds.

Oligomerization of the known catalyst is typically carried out in a hydrocarbon solvent medium at a temperature of from about 100 to 150 ° C and a pressure increase of 4-8 MPa.

However, the main disadvantage of this known catalyst is that the solubility of zirconium tetrachloride in a hydrocarbon solvent is poor, the conditions of the catalyst operation are severe and the selectivity is relatively low. In the ethylene oligomerization process, a large amount of wax and up to 3.0% by weight of high molecular polyethylene are formed together with the linear alpha olefin.

No. 4,783,573 discloses a zirconium/aluminum complex-based catalyst system which is formed using anhydrous zirconium chloride with aluminum sesquichloride and triethylaluminum in an anhydrous benzene solvent. These components are stirred under argon for a period of time to form an active catalyst complex. The addition of thiophene to the catalyst is presumed to be a regulator.

A patented example of oligomerization in anhydrous benzene at 120 ° C, 3.4 MPa, shows the ability to produce alpha-olefins having a long chain length, and the results are as follows: C _{4 -} 14.9% by weight, C _{6 -} 15.1% by weight, C ₈ -14.0% by weight, C ₁₀ -C ₁₈ -40.2% by weight, C _{20+ -} 14.2% by weight, and wax - 1.6% by weight. A disadvantage of this process is the high yield of C ₂₀₊ alpha-olefins. Another disadvantage is the high reaction temperature. Another disadvantage of this method is that benzene used as a solvent is a known carcinogen.

The use of alcohols (methanol and/or ethanol) as a third component is disclosed in US 5,260,500 to produce high purity alpha-olefins free of contaminants. A disadvantage of this system is the high yield of the C20 ₊ fraction.

A nickel-based catalyst system is disclosed in EP 0 953 556 B1, in which a linear alpha olefin oligomer produced by adding water as a catalyst system to a polar organic liquid in a process of ethylene oligomerization The substance is higher in purity than the one formed in the absence of water. According to this patent, 95.05 wt% of the terpene moiety is terpene-1 in the absence of water; 95.99 wt% of the terpene moiety is terpene-1 in the presence of cyclobutanide containing about 1.0 wt% water.

Furthermore, WO 80/00224 and DE 4338414 also disclose a catalyst comprising a zirconium carboxylate of the formula (RCOO) _m ZrCl _4-m and an organoaluminium compound of the formula R _n AlX _3-n . A major disadvantage of this catalyst system is the formation of unintended and problematic by-products such as waxes and/or polymers (polyethylene, branched and/or crosslinked PE). Another disadvantage of this catalyst system is the high catalyst/activator consumption. The catalyst/cocatalyst ratio is a key parameter that enables adjustment of the alpha-olefin distribution. The catalyst/cocatalyst ratio is highly conducive to the production of low molecular weight oligomers at the expense of the C10 ₊ moiety of the branch.

The formation of waxes and/or polymers, even in small amounts, has a detrimental effect on the overall process of making the oligomers, as by-products not only reduce the yield and purity of the desired oligomers, but also reduce the operating time of the process equipment, Since the solid polymer accumulated in the reactor must be periodically removed, it can only be carried out while the oligomerization process is suspended, at the expense of equipment time loss.

Therefore, there is currently a large need to develop an improved catalyst system that provides equal or even greater catalyst activity while eliminating all or at least some of the above problems and reducing the cost of the last catalyst.

Accordingly, it is an object of the present invention to provide a catalyst composition which overcomes the deficiencies of the prior art and, more particularly, to provide a wax which enables the purity of the produced α-olefin to be high while forming a reactor. / Catalyst composition with minimal polymer. In particular, an α-olefin having 6 to 10 carbon atoms is provided.

Further, there is provided a process for producing a linear α-olefin by oligomerization of ethylene, and a process for preparing the catalyst composition.

The first object is achieved by a catalyst composition of oligoethylene comprising: (i) at least partially hydrolyzed transition metal compound by adding water to the control in a controlled manner A transition metal compound having the formula MX _m (OR') _4-m or MX _m (OOCR') _4-m wherein R' is an alkyl group, an alkenyl group, an aryl group, an arylalkyl group or a cycloalkyl group; X is a halogen, preferably Cl or Br; and m is 0 to 4, preferably 0 to 3; and (ii) an organoaluminum compound as a promoter, wherein the molar ratio of water to the transition metal compound It is in the range of about 0.01:1 to 3:1.

The molar ratio of the water to the transition metal compound is preferably in the range of from about 0.1:1 to 2:1.

The transition metal compound is more preferably a zirconium compound.

The zirconium compound is preferably a zirconium carboxylate having the formula (R ² COO) _m ZrCl _4-m wherein R ² is an alkyl group, an alkenyl group, an aryl group, an arylalkyl group or a cycloalkyl group, and m is at 0. Any number within the range of 4.

In a specific embodiment, the organoaluminum compound has the formula R ¹ _n AlZ _3-n or Al ₂ Z ₃ R ¹ ₃ wherein R ¹ represents an alkyl group having 1 to 20 carbon atoms; Z represents Cl, Br or I; n is in the range 1 n Any number within 2.

The organoaluminum compound is preferably Al(C ₂ H ₅ ) ₃ , Al ₂ Cl ₃ (C ₂ H ₅ ) ₃ , AlCl(C ₂ H ₅ ) ₂ or a mixture thereof. According to a more preferred embodiment of the invention, the organoaluminum compound is ethylaluminum sesquichloride and/or diethylaluminum chloride.

Further, the molar ratio of the organoaluminum compound to the transition metal compound is preferably in the range of 1:1 to 40:1.

The transition metal compound is more preferably hydrolyzed.

According to the present invention, it is also a process for preparing a linear alpha-olefin by the presence of an organic solvent and an oligomeric polyethylene of the catalyst composition of the present invention.

Also provided is a method of preparing a catalyst composition of the present invention comprising the steps of: (i) adding water to a transition metal compound in a controlled manner, wherein the transition metal compound is provided as a solution; and (ii) the organoaluminum The compound is combined with a solution of at least partially hydrolyzed transition metal compound.

Wherein the water in step (i) is added incrementally, such as in the form of water vapor, in a divided or continuous manner, preferably in drops, or by release from aqueous solids.

More preferably, the solution is stirred for 1 minute to 60 minutes, preferably 1 minute to about 30 minutes, preferably at room temperature, during or after the addition of water.

Surprisingly, it has been found that controlling the amount of water added to at least partially hydrolyze the transition metal compound (preferably a zirconium compound) improves the catalyst composition and provides an alpha-olefin of higher purity in the reactor. Wax/polymer formation is also minimized. The transition metal compound is partially hydrolyzed by using a controlled amount of water as a regulator. In particular, the combination of a zirconium catalyst precursor and a chlorinated organoaluminum compound as a cocatalyst will selectively oligomerize ethylene to form a high purity linear alpha olefin and the formation of the polymer/wax is evident. reduce.

Furthermore, the catalyst composition also exhibits high activity and productivity, and can be produced in a desired molecular weight range (i.e., C ₄ -C) only by a relatively low amount of catalyst compared to prior art catalysts. ₂₀ range, and in order for the preferred C ₆ -C ₁₀₎ linear olefins.

Furthermore, the operating time of the process equipment can be extended and the cost of clearing the solid polymer buildup in the reactor can be reduced. Therefore, production batches can be increased.

For those skilled in the art, the meaning of the term "partial hydrolysis" is clearly understood. In detail, using a transition metal compound as a starting material, after very careful addition of water, the transition metal compound is hydrolyzed, that is, the alkanol or carboxylic acid group (at least a part) is removed from the metal (possibly formed separately). ROH or ROOH is off the base). In other words, the molar ratio of the above water to the transition metal compound is the molar ratio of the water and the transition metal starting compound added in a controlled manner.

The catalyst composition used in the method for producing a linear α-olefin is preferably present in an inert organic solvent. Examples of suitable organic solvents include unsubstituted or halogen-substituted aromatic hydrocarbon solvents such as toluene, benzene, xylene, chlorobenzene, dichlorobenzene, chlorotoluene, etc.; aliphatic paraffin hydrocarbons such as pentane, hexane , heptane, octane, decane, decane, etc.; alicyclic hydrocarbon compounds such as cyclohexane, decalin, etc.; halogenated alkanes such as dichloroethane, dichlorobutane and the like. The product molecular weight distribution can be controlled using a mixture of solvents to achieve maximum selectivity to the desired olefin product.

The specific hydrolysis ratio (moth ratio of water to transition metal compound) can be used to control the degree of hydrolysis. This hydrolysis ratio affects the reaction rate. Furthermore, the mode of adding water to the transition metal compound solution does affect the rate of hydrolysis. For example, immediately after the addition of water, clustered particles are produced, or no visible particle formation occurs, depending on the method of addition.

There are several factors that can affect the rate of hydrolysis, such as the nature of the organic group, the number of metal coordination, the functionality of the precursor, and the like. The hydrolysis reaction itself can be supplied directly Controlled by the amount of water and the rate of addition of the transition metal compound. The water may be supplied intermittently, or in a staged or continuous manner, and the overall addition does not result in the desired reaction, resulting in precipitation of excess hydrolysis in combination with insolubles. There are various ways to add water. A preferred method is to carry out the dropwise addition of the solution in which the transition metal compound is dissolved in the hydrocarbon while stirring. Stirring time is important in order to have the desired result. The stirring time may be in the range of from 1 minute to 60 minutes, preferably from about 1 minute to about 30 minutes, and more preferably at room temperature.

Additionally, the water can be added using a stream of nitrogen to introduce water vapor into the reaction. Aqueous solids may also be used, which may be hydrated materials or porous materials that have absorbed moisture.

Therefore, it is necessary to control the addition of water, and the total amount of water cannot be added in a general manner, that is, it is not fed once, but must be carefully added in a controlled manner to particularly prevent the formation of precipitates.

In a preferred embodiment, metered water is added dropwise to the solution of the transition metal compound using a syringe at room temperature. When water is added, it is preferred to simultaneously stir the mixture. Depending on the amount of water, some precipitation may be observed due to hydrolysis when water is added. Usually, no precipitation is observed after stirring.

The catalyst composition of the present invention can be utilized in a process for preparing a linear alpha olefin at a reaction temperature of from about 50 ° C to about 110 ° C, preferably from about 60 ° C to about 100 ° C.

The Zr metal concentration (% by weight) in the zirconium compound may vary from 2% by weight to 10% by weight, and preferably from 3% by weight to 7% by weight.

This oligomerization can be carried out under ordinary reaction conditions (e.g., temperature, pressure, etc.) known to those skilled in the art.

Further features and advantages of the present invention will become apparent from the following detailed description of the preferred embodiments.

Experimental conditions:

All materials were operated under nitrogen using Schlenk techniques or a nitrogen filled glove box. Nitrogen and toluene are supplied from the factory source and can be dried by additional molecular sieve beds as needed.

Example

The synthesis of zirconium carboxylate is carried out in accordance with known methods.

The oligomerization of ethylene was carried out in the following steps: The oligomerization was carried out in a 2 liter stainless steel reactor. The prepared catalyst solution was added to the reactor. Ethylene was poured into the reactor until the desired pressure was obtained and the expected temperature was maintained throughout the reaction. The ethylene is continuously introduced in an amount sufficient to maintain the reaction pressure. After continuing to react for 1 hour and maintaining the reaction conditions, the ethylene supply was interrupted and the reaction was stopped by adding about 20 ml of ethanol. After adjusting the temperature of the reaction mixture to 10 ° C, the solution sample was collected by a valve located at the bottom of the reactor, and analyzed by gas chromatography to determine the amount and type of olefin formed. After removing the excess pressure of ethylene, the reactor was opened to detect any possible polymer formation. The yield of the C ₄ -C ₆ fraction was estimated from the Schulz-Flory distribution because there was inevitably some loss in handling the sample.

Example 1

In a solution of Zr(iC ₃ H ₇ COO) ₄ (1.25 mmol) dissolved in toluene (3.25 mL), water was poured dropwise to obtain H ₂ O/Zr = 0.44. This mixture was stirred at room temperature for 15 minutes. Then, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ was extracted from the solution and added to 200 ml of toluene placed in a 250 ml round bottom flask. Pure EASC (Al/Zr = 17.5) was then added to the mixture. The catalyst solution thus formed is then transferred to the reactor under an inert gas stream. The reaction was carried out at 80 ° C and 30 bar of ethylene pressure. The oligomerization time was 60 minutes. 193 g of LAO was formed; the yield of LAO was 8465 g LAO/g Zr. A clear liquid is obtained. No wax formation was observed in the product. Only traces of solid polymer were detected, that is, because the content was too low to be accurately determined.

Example 2

In a solution of Zr(iC ₃ H ₇ COO) ₄ (1.25 mmol) in toluene (3.25 mL), water was poured dropwise to give H ₂ O/Zr = 1.08. This mixture was stirred for 15 minutes. Then, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ was extracted from the solution and added to 200 ml of toluene placed in a 250 ml round bottom flask. Pure EASC (Al/Zr = 17.5) was then added to the mixture. The catalyst solution so formed is then transferred to the reactor under an inert gas stream. The reaction was carried out at 80 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 173 g of LAO was formed; the yield of LAO was 7588 g LAO/g Zr. A clear liquid is obtained. No wax formation was observed in the product. Only traces of solid polymer were detected, that is, because the content was too low to be accurately determined.

Example 3

In a solution of Zr(iC ₃ H ₇ COO) ₄ (1.25 mmol) in toluene (3.25 mL), water was poured dropwise to give H ₂ O / Zr = 1.32. This mixture was stirred for 15 minutes. Then, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ was extracted from the solution and added to 200 ml of toluene placed in a 250 ml round bottom flask. Pure EASC (Al/Zr = 17.5) was then added to the mixture. The catalyst solution so formed is transferred to the reactor under an inert gas stream. The reaction was carried out at 80 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 162 g of LAO was formed; the yield of LAO was 7105 g LAO/g Zr. A clear liquid is obtained. No wax/polymer formation was observed.

Example 4

In a solution of Zr(iC ₃ H ₇ COO) ₄ (1.25 mmol) in toluene (3.25 mL), water was poured dropwise to give H ₂ O/Zr = 0.44. This mixture was stirred for 15 minutes. Then, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ was extracted from the solution and added to 200 ml of toluene placed in a 250 ml round bottom flask. Pure EASC (Al/Zr = 35) was then added to the mixture. The catalyst solution so formed is then transferred to the reactor under an inert gas stream. The reaction was carried out at 80 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 155 g of LAO was formed; the yield of LAO was 6798 g LAO/g Zr. A clear liquid is obtained. No wax/polymer formation was observed.

Example 5

In a solution of Zr(iC ₃ H ₇ COO) ₄ (1.35 mmol) in toluene (3.25 mL), water was poured dropwise to give H ₂ O /Zr = 0.82. This mixture was stirred for 15 minutes. Then, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ was extracted from the solution and added to 200 ml of toluene placed in a 250 ml round bottom flask. Pure EASC (Al/Zr = 17.5) was then added to the mixture. The catalyst solution thus formed is transferred to the reactor under an inert gas stream. The reaction was carried out at 70 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 186 g of LAO was formed; the yield of LAO was 8157 g LAO/g Zr. A clear liquid is obtained. No wax/polymer formation was observed.

Example 6

Water was poured into a solution of Zr(iC ₃ H ₇ COO) ₄ (6.25 mmol) in toluene (11 ml) to give H ₂ O/Zr = 0.68. This mixture was stirred for 15 minutes. Then, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ was extracted from the solution and added to 200 ml of toluene placed in a 250 ml round bottom flask. Pure EASC (Al/Zr = 17.5) was then added to the mixture. The catalyst solution thus formed is then transferred to the reactor under an inert gas stream. The reaction was carried out at 75 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 245 g of LAO was formed; the yield of LAO was 10745 g LAO/g Zr. A clear liquid is obtained. No wax/polymer formation was observed.

Example 7

After 1 month, the same hydrolyzed zirconium catalyst solution prepared in Example 6 was tested using the same procedure as described in Example 6 (mixing the sample for 1 minute before taking the required amount) to verify its remanufacturability ( Reproducibility). If the catalyst solution is stored for a longer period of time, it may be necessary to periodically agitate the solution to prevent precipitation. 234 g of LAO was formed; the yield of LAO was 10263 g LAO/g Zr. A clear liquid is obtained. No wax/polymer formation was observed.

Comparative example 1

200 ml of toluene, 0.25 mmol of Zr(iC ₃ H ₇ COO) ₄ and neat ethylaluminum sesquichloride (EASC) (Al/Zr = 35) were mixed in a 250 ml round bottom flask. The catalyst solution thus formed is then transferred to the reactor under an inert gas stream. The reaction was carried out at 80 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 213 g of LAO was formed; the yield was 9342 g LAO/g Zr. A small amount of solid polymer was observed.

Comparative example 2

The same steps as in Comparative Example 1 were repeated except that Al/Zr = 17.5. The reaction was carried out at 80 ° C and 30 bar ethylene pressure. The oligomerization time was 60 minutes. 460 g of LAO and 0.2 g of by-product polyethylene were formed; the yield was 20175 g LAO/g Zr. A high level of wax is formed which cannot be accurately analyzed by GC.

Comparative example 3

The same procedure as in Comparative Example 1 was repeated except that a set amount of water was intentionally added to toluene and 20 ppm of water was used in toluene. 153 g of LAO was formed; the yield was 6710 g LAO/g Zr. The results of this experiment show that the purity of the product is drastically reduced (mainly due to the Friedel-Crafts alkylation reaction of toluene). At the same time, a significant increase in polymer formation was observed, the main It is deposited on the reactor wall, the stirrer and the thermowell.

Table 1 below summarizes the chain length distribution of the obtained α-olefin, and Table 2 summarizes the purity of the obtained LAO- moiety.

From the above table, it was found that the catalyst composition according to the present invention can obtain an α-olefin distribution having a high content of the intended C ₆ -C ₁₀ α-olefin. As shown in Table 2, the purity of the fraction obtained by the catalyst composition according to the present invention was also remarkably improved.

The features disclosed in the above description and claims are intended to be inclusive or in any combination.

Claims (8)

A catalyst composition for oligoethylene to be a C ₆ -C ₁₀ linear oligomer comprising: (i) at least partially hydrolyzed transition metal compound by adding water in a controlled manner To a transition metal compound of the formula MX _m (OOCR') _4-m wherein R' is alkyl, alkenyl, aryl, aralkyl or cycloalkyl; X is halogen; and m is 0 to And (ii) an organoaluminum compound as a cocatalyst, wherein the molar ratio of water to the transition metal compound is in the range of from about 0.01:1 to 3:1; wherein the transition metal compound is a zirconium compound. The catalyst composition of claim 1, wherein the halogen is Cl. The catalyst composition of claim 1, wherein the molar ratio of water to the transition metal compound is in the range of from about 0.1:1 to 2:1. The catalyst composition of claim 1, wherein the zirconium compound is a zirconium carboxylate having the formula (R ² COO) _m ZrCl _4-m , wherein R ² is an alkyl group, an alkenyl group, an aryl group, or an aromatic group. Alkyl or cycloalkyl, and m is any number in the range of 1 to 4. The catalyst composition of claim 1, wherein the organoaluminum compound is Al(C ₂ H ₅ ) ₃ or has the formula R ¹ _n AlZ _3-n or Al ₂ Z ₃ R ¹ ₃ , wherein R ¹ represents an alkyl group having 1 to 20 carbon atoms; Z represents Cl, Br or I; n is in the range 1 n Any number within 2. The catalyst composition of claim 5, wherein the organoaluminum compound is Al ₂ Cl ₃ (C ₂ H ₅ ) ₃ , AlCl(C ₂ H ₅ ) ₂ or a mixture thereof. The catalyst composition of claim 1, wherein the molar ratio of the organoaluminum compound to the transition metal compound is in the range of 1:1 to 40:1. The catalyst composition of claim 1, wherein the transition metal compound is partially hydrolyzed.