Patent Application
20160145360
The invention is directed to a process for the production of polyethylene by polymerisation of ethylene in the presence of a chromium oxide based catalyst.
The production processes of LDPE, HDPE and LLDPE are summarised in “Handbook of Polyethylene” by Andrew Peacock (2000; Dekker; ISBN 0824795466) at pages 43-66. The catalysts can be divided in three different subclasses including Ziegler Natta catalysts, Phillips catalysts and single site catalysts. The various processes may be divided into solution polymerisation processes employing homogeneous (soluble) catalysts and processes employing supported (heterogeneous) catalysts. The latter processes include both slurry and gas phase processes.
The chromium oxide based catalyst, which is commonly referred to in the literature as “the Phillips catalyst”, can be obtained by calcining a chromium compound carried on an inorganic oxide carrier in a non-reducing atmosphere. The chromium oxide catalysis and the ethylene polymerisation with this specific catalyst are disclosed in “Handbook of Polyethylene” by Andrew Peacock at pages 61-64.
Polyethylene is suitable to be applied in the production of blow moulded articles via the so-called “blow moulding technique”. In fabricating blow moulded articles, for example milk bottles, a balance between the physical properties and the processing properties of the polymer, for example polyethylene, must be present. Because of the physical properties of the manufactured article, the density of the polymer from which the article is manufactured has to be as high as possible because a high density results in a high rigidity of the article to make it possible to produce, for example, a bottle, being resistant to deformation. Due to the higher rigidity it is possible to obtain a product having the desired requirements and additionally having thinner walls so that savings in the consumption of (poly)ethylene are achieved. Because of the processing properties the polymer must have good flow properties. The higher the flow of the polymer, the faster the articles may be produced
Very important are the mechanical properties of the polymer by means of Environmental Stress Crack Resistance (ESCR). As disclosed in “Handbook of Polyethylene, structure, properties and applications” (by Andrew Peacock, Dekker, New York, 2000; pages 124-170) high density polyethylene (homopolymer and copolymer) is rather tough at room temperature. However, due to its viscoelastic nature, a high density polyethylene (HDPE) article loses shape stability when subjected to prolonged stress. This is the case even when the applied stress is much lower than the stress required to induce plastic deformation (yield stress, σy). Mechanical instability can manifest itself in the form of creep, stress relaxation, crazing and/or environmental stress cracking. All these long-term instabilities involve gradual rearrangement of molecules either on a local level (in the case of brittle failure and stress cracking) or throughout a large portion of the sample (as in creep and stress relaxation). When exposed to stresses of less than one half the yield stress and if bulk inhomogeneity is present, brittle failure (no macroscopic orientation prior to failure) occurs by slow crack growth. The crack is initiated at an existing stress concentration point (bulk inhomogeneity) such as for example a sharp notch or a scratch. The resistance offered by a polymer to fracture in a certain environment and at a certain stress is an important resin property and referred to as ESCR. ESCR is the accepted criterion of long-term durability of HDPE products (notably blow moulding items and pipes) exposed to elevated pressure and temperature, chemicals and/or stresses. ESCR may be measured by an accelerated testing method which measures the time needed for a notched material to fail under slow crack propagation conditions (low applied stress) at elevated temperatures and in the presence of a surfactant without changing the failure mechanism. Slow crack propagation in ethylene based polymers proceeds via crazing. A pre-crack (scratch or notch) leads to stress concentration, which results in the formation of the deformation zone (or yield zone). This zone consists of miniscule cavities (voids), which will grow and join up to form an essentially fibrillar structure usually referred to as craze. The fibrils within a craze will extend over time until a failure criterion is satisfied and consequently the material will fail. This process of fibrillar extension and subsequent weakening is generally accepted to be a rate-determining step controlling the overall slow crack propagation in polyethylene. This step is governed by the disentanglement process of (tie) molecules. The more tie molecules present, the more stress can be supported and consequently the higher the resistance against a chain detaching from a crystal. On the other hand, the ability of releasing a chain from a crystal will also highly depend on crystal strength, which is determined by the crystal's perfection and thickness. Given this slow crack propagation mechanism in polyethylene, the molecular parameters leading to high ESCR are the same parameters which will lead to an increased number of tie molecules. On the other hand it is desirable that the finished products also retain desirable stiffness, which is predominantly determined by crystallinity and/or crystal size. The two requirements for the desired molecular structure (high crystallinity and a large number of tie molecules) are conflicting as the formation of an increased number of tie molecules will result in lower crystallinity (i.e. lower stiffness). Polyethylene having a lower density possesses a higher ESCR. The density of polyethylene may be controlled by the addition of an α-olefine, which leads to products possessing short chain branching. The incorporation of short chain branches will enhance ESCR by forcing molecules to crystallize in different lamellar crystals and consequently leads to an increased number of tie molecules. This is especially the case if short chain branches are predominantly incorporated in the long molecular chains. When for example HDPE is produced in a single reactor system with a heterogeneous catalyst system, such as for example a chromium-containing or a Ziegler Natta system, the comonomers may be incorporated in the low molar mass tail and their amount will decrease with increasing molar mass values. This heterogeneous comonomer distribution with respect to molar mass distribution is not favourable for high ESCR and high stiffness. A highly branched low molar mass tail will not effectively contribute to the formation of effective tie molecules but at the same time it will lead to a dramatic decrease in density and therefore in the resulting stiffness. Highly linear long chains will form tie molecules, which will not be as effective as those containing branches, as the slip through the crystal will be much more facilitated. On being extruded through the die, the polymer melts exhibit so-called die swell. This phenomenon is a drawback during processing, for example during blow moulding of for example thin bottles and/or containers. Therefore an easily processable polymer also exhibits low die swell. More than 65% of the blow moulding market utilizes HDPE obtained by a process using a chromium catalyst and the problem of these grades during processing is their relatively high die swell. This is due to their enhanced melt elasticity, which results from molecular as well as rheological broadness, the latter being a consequence of the ability of a chromium-containing catalyst to develop the low degree of long chain branching.
The strain hardening modulus is a measure of environmental stress crack resistance of high density polyethylene. The strain hardening modulus of polyethylene was measured by the method as described by Kurelec in Elsevier, Polymer 46 (2005) p. 6369-6379.
It is the object of the present invention to provide polyethylene having the desired ESCR or strain hardening modulus values to be applied in the production of bottles.
The present invention relates to a process for the production of high density polyethylene in the presence of a catalyst composition comprising a porous silicon oxide support material carrying a chromium compound and a transition metal containing compound or metal halide transition metal compound wherein the silicon oxide support material has an average particle size between 20 um and 40 um, a pore volume between 1.8 and 2.2 ml/g and a surface area between 400 and 600 m2/g.
A suitable pore diameter for the silica used may be for example about 146 Angstrom as an average to the size of the opening of the pore.
The process according to the present invention results in improved mechanical properties especially the ESCR/ strain hardening modulus. This improvement results in excellent bottles suitable to be used as a container for detergents, chloric, bleaches and liquid soap were these chemicals known to have a damaging corrosive effect on plastics.
The process according to the present invention results in improved morphology, improved bulk density, less fines and improvement in C6 co-monomer incorporation.
For the production of bottles for foodstuffs, for example milk, there exist requirements with respect to smell and/or taste. The process according to the invention does not result in compounds that adversely influence the taste and smell.
In the catalyst composition the chromium compound which is activated in the calciner to turn into CrO3 “active sites” for ethylene polymerization is the precursor. The chromium compound can be selected from various organic and inorganic forms of chromium. Preferably the chromium compound is selected from chromium acetate, chromium acetyl acetonate, chromium acetate hydroxide and chromium trioxide. Most preferably chromium acetate or chromium acetyl acetonate is applied.
According to a preferred embodiment of the invention the average particle size ranges between 25 um and 35 um.
According to a preferred embodiment of the invention the surface area ranges between 480 and 545 m2/g.
According to a further preferred embodiment of the invention the surface area ranges between 480 and 525 m2/g.
According to a preferred embodiment of the invention the transition metal compound or metal halide transition metal compound has the general formula Tm (OR1)nX4-n and Tm (R2)nX4-n, wherein
The transition metal may be titanium, vanadium, hafnium or zirconium.
According to a preferred embodiment of the invention the metal is titanium.
Suitable examples of R1 include (C1-C20) alkyl groups for example methyl, ethyl, n-propyl, isopropyl and n-butyl groups.
Preferably the halogen atom is chlorine.
Preferably the transition metal compound or metal halide transition metal compound has the formula Tm (OR1)nX4-n
Examples of suitable titanium compounds having the general formula Tm (OR1)nX4-n and Tm (R2)nX4-n include titanium alkoxy compounds for example tetraethoxy titanium, tetramethoxy titanium, tetrabutoxy titanium, tetrapropoxy titanium, tetraisobutoxy titanium, tetrapentoxy titanium, triethoxychloro titanium, diethoxydichloro titanium , trichloethoxy titanium, methoxy titanium trichloride, dimethoxy titanium dichloride, ethoxy titanium trichloride, diethoxy titanium dichloride, propoxy titanium trichloride, dipropoxy titanium dichloride, butoxy titanium trichloride, butoxy titanium dichloride, titanium tetrachloride, vanadium trichloride, vanadium tetrachloride, vanadium oxytrichloride, zirconium tetrachloride and/or vanadium tetrachloride .
The amount of chromium in the final catalyst is less than 0.5% by weight. More preferably the amount of chromium in the final catalyst ranges between 0.1 and 0.4% by weight.
The metal continent, preferably the titanium content, of the catalyst ranges between 3.0 and 4.0% by weight.
The catalyst composition may also comprise a magnesium containing compound.
The catalyst composition may also comprise an organoaluminium containing compound.
The process according to the invention may be applied for ethylene polymerization to medium and high density polyethylene and copolymers of ethylene with alpha-olefins having about 3 to 18 carbon atoms.
According to a preferred embodiment of the invention the comonomer is 1-hexene.
The produced polyethylene may be HDPE and LLDPE.
According to a preferred embodiment of the invention the polymerisation takes place via a gas phase polymerisation process.
A gas phase reactor is essentially a fluidized bed of dry polymer particles maintained either by stirring or by passing gas (ethylene) at high speeds through it. The obtained powder is mixed with stabilizers and generally extruded into pellets. Gas fluidized bed polymerisation processes are summarised by Than Chee Mun in Hydrocarbons 2003 “Production of polyethylene using gas fluidised bed reactor”. Gas phase polymerisation generally involves adding gaseous monomers into a vertically oriented polymerisation reactor filled with previously formed polymer, catalyst particles and additives. Generally the polymerisation in the gas phase polymerisation systems takes place at temperatures between 30° C. and 130° C. with super atmospheric pressures. The rising gas phase fluidizes the bed, and the monomers contained in the gas phase polymerize onto supported catalyst or preformed polymer during this process. Upon reaching the top of the reactor, unreacted monomer is recycled, while polymer continually falls down along the sides of the reactor. Examples of suitable gas phase polymerisations are disclosed in for example U.S. Pat. No. 4,003,712 and US-A-2005/0137364.
The catalyst composition comprising the porous silica support material carrying a chromium salt and the transition metal containing compound or metal halide transition metal compound may be prepared by adding the chromium salt to the silica support in a suitable solvent like methanol or ethanol then the slurry is mixed and dried at about for example 85° C.
The polyethylene powder obtained with the catalyst composition according to the present invention has:
According to a preferred embodiment of the invention the polyethylene powder obtained with the catalyst composition according to the present invention has:
The obtained polyethylene is suitable to be applied in the production of large-part blow molded articles and especially for milk bottles and house industrial containers.
The ethylene polymers obtained with the process according to the invention may be combined with additives such as for example lubricants, fillers, stabilisers, antioxidants, compatibilizers and pigments. The additives used to stabilize the polymers may be, for example, additive packages including hindered phenols, phosphites, UV stabilisers, antistatics and stearates.
WO 2008/045171 A2 discloses a supported olefin polymerization catalyst having a silica surface area ranging between 264 m2/g up to 336 m2/g whereas the surface area of the silica in the present invention ranges between 400 and 600 m2/g.
U.S. Pat. No. 5,115,053 discloses a silica support having am average particle size in the range between 70 and 90 μm. Because of the narrow control on average particle size and morphology the present invention is able to produce upper fluidized bulk density >280 kg/m3 in fluidized gas phase reactor which does not correlate with the slurry loop process as applied in U.S. Pat. No. 5,115,053.
The invention will be elucidated by means of the following non-limiting examples.
The properties of the polymers produced in the Examples were determined as follows:
To a three-necked round bottom flask, equipped with a condenser and a mechanical stirrer 30 g of dried silica (M-203-F silica support) with 0.5% Cr average particle size of 35 micrometres, a surface area (SA) of 519 m2/g and a pore volume (PV) of 1.9 ml/g at 200° C. is placed into the flask then 0.57 g of Chromium acetate hydroxide were added to the silica then slurried in 250 cm3 of Methanol (100%), which was stirred at 70° C. for 60 minutes. After wards drying ethanol solvent took place at 85° C. with nitrogen purge. The dried chromium salt on silica powder was cooled down to room temperature then slurried with 250 cm3 of iso-pentane, to be followed by the addition of 8.6 cm3 of 100% Ti(OC2H5)4 (tetra ethoxy titanium) which was allowed to mix for 30 minutes at 45° C. then drying the solvent at 75° C. with nitrogen purge. For the chrome catalyst activation the dried catalyst powder was placed in the calciner and the following sequence was followed:
Elemental analysis: 0.35 wt % Cr and 4.1 wt % Ti
Figure I shows the catalyst from Example I.
Synthesis of Catalyst Composition
To a three-necked round bottom flask, equipped with a condenser and a mechanical stirrer 30 g of dried silica with 0.5% Cr average particle size of 45 micrometres, a pore volume (PV) of 1.5 ml/g and a surface area (SA) of 310 m2/g at 200° C. slurried with 250 cm3 of iso-pentane, to be followed by the addition of 6.8 cm3 of tetraethoxy titanium Ti(OC2H5)4 (100%). The contents were mixed at 35° C. for another 60 minutes followed by drying the solvent at 85° C. with nitrogen purge. For the chrome catalyst activation the dried catalyst powder was placed in the calciner and was activated in air at 800 ° C. for 4 hours.
Elemental analysis: 0.38 wt % Cr and 3.8 wt % Ti.
Ethylene Polymerization
An autoclave with a volume of 2 liters was purged with nitrogen at 130° C. for 30 minutes. After cooling the autoclave to 70° C., one liter of iso-pentane and 10 ml of 1-hexene were introduced to the reactor. The reactor was pressurized with 15 bar ethylene. Then 0.1 mmol of TEAL was injected into the reactor by the means of a catalyst injection pump. This was followed by injection of 0.15 g of catalyst composition according to Example I after being slurried in 20 cm3 of iso-pentane solvent. The reactor temperature was raised to 106° C. Ethylene polymerization was carried out for 60 minutes; with ethylene supplied on demand to maintain the total reactor pressure at 20 bar. 388 litres of ethylene were consumed and 363 grams of polyethylene were recovered giving a catalyst productivity of 2,420 g PE/g cat h at 200 psig.
The characteristics of the obtained polyethylene:
Ethylene Polymerization
An autoclave with a volume of 2 litres was purged with nitrogen at 130° C. for 30 minutes. After cooling the autoclave to 70° C., one litre of iso-pentane and 10 ml of 1-hexene were introduced to the reactor. The reactor was pressurized with 15 bar ethylene.
Then 0.1 mmol of TEAL was injected into the reactor by the means of a catalyst injection pump. This was followed by injection of 0.15 g of catalyst composition according to Comparative Example A after being slurried in 20 cm3 of iso-pentane solvent. The reactor temperature was raised to 101° C. Ethylene polymerization was carried out for 60 minutes; with ethylene supplied on demand to maintain the total reactor pressure at 20 bar.
329 litres of ethylene were consumed and 318 grams of polyethylene was recovered giving a catalyst productivity of 2,120 g PE/g cat h at 200 psig.
The characteristics of the obtained polyethylene:
The results from Example II in comparison to Example B show better productivity and resin bulk density because of the use of the catalyst prepared in Example I.
Ethylene Gas Phase Polymerization
Ethylene was polymerised in the presence of the catalyst according to Example I via a gas phase polymerisation with reactor pressure: 20.7 bar, bed temperature 108° C., bed weight 55 kg; C2 partial pressure: 15 bar; C6/C2 ratio 0.0008; H2/C2 ratio 0.16 and super gas velocity (S.G.V) 0.44 m/sec.
The production rate was 12 kg/h and the catalyst productivity 10,000 kg/kg
The characteristics of the obtained polyethylene:
Figure II shows the HDPE from Example III.
Ethylene Gas Phase Polymerization
Ethylene was polymerised in the presence of the catalyst according to Comparative Example A via a gas phase polymerisation with reactor pressure: 20.7 bar, bed temperature 108° C., bed weight 51 kg; C2 partial pressure: 15 bar; C6/C2 ratio 0.00125; H2/C2 ratio 0.16 and S.G.V 0.41 m/sec
The production rate was 10.5 kg/h and the catalyst productivity 10,000 kg/kg
The characteristics of the obtained polyethylene:
When comparing Example III and Comparative Example C we note that the catalyst system according to Example I produces a resin of increased bulk density, accordingly bed weigh in the reactor was increased (from 51 kg up to 55 kg) which causes an increase in the drop size, eventually increasing the production rate which is very significant for gas phase polymerisation.
The strain hardening modulus according to Example III is improved in comparison with strain hardening modulus according to Comparative Example C.
C6/C2 was increased to 0.00125 to produce a density of 954 kg/m3 and only 0.0008 C6/C2 ratio was used to produce a density of 953 kg/m3
| Number | Date | Country | Kind |
|---|---|---|---|
| 13173418.8 | Jun 2013 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2014/062716 | 6/17/2014 | WO | 00 |
| Number | Date | Country | |
|---|---|---|---|
| 61929759 | Jan 2014 | US |
