FORM-2
THE PATENTS ACT, 1970
(39 of 1970)
&
THE PATENTS RULES, 2003
COMPLETE SPECIFICATION
(See Section 10 and Rule 13)
A PROCESS FOR SYNTHESIS OF ETHYLENE POLYMERS
RELIANCE INDUSTRIES LTD.
An Indian Company
Of 3rd Floor, Maker Chamber - IV, 222, Nariman Point,
Mumbai 400 021, Maharashtra, India.
NAME OF THE INVENTORS
1. SARMA KRISHNA RENGANATH
2. MATHUR AJIT BEHARI
3. JASRA RAKSHVIR
4. SHASHIKANT
5. PADMANABHAN SUDHAKAR
6. PATEL VIRALKUMAR
THE FOLLOWING SPECIFICATION PARTICULARLY DESCRIBES THE INVENTION AND THE MANNER IN WHICH IT IS TO BE PERFORMED

FIELD OF THE INVENTION
The present invention relates to synthesis of polyethylene.
Particularly, the present invention relates to synthesis of disentangled ultra high molecular weight polyethylene (DUHMWPE).
BACKGROUND
Ultra high molecular weight polyethylene (UHMWPE) is a type of polyolefin. It is made up of extremely long chains of polyethylene. It derives its strength largely from the length of each individual molecule (chain). Van der Waals bonds between the molecules are relatively weak for each atom of overlap between the molecules, but because the molecules are very long, large overlaps can exist, adding up to the ability to carry larger shear forces from molecule to molecule. Each chain is bonded to the others with so many Van der Waals bonds that the whole of the inter-molecule strength is high.
The polar groups present in most polymers easily bond with water. UHMWPE does not absorb water readily as polar groups are absent in it which makes its bonding with other polymers difficult. Therefore, skin does not interact with it strongly, making the UHMWPE fiber surface feel slippery. As UHMWPE does not contain chemical groups such as esters, amides or hydroxylic groups, that are susceptible to attack from aggressive agents, it is very resistant to water, moisture, most chemicals. UV radiation, and micro-organisms. UHMWPE are immune to aromatic stacking interactions caused in contact with aromatic solvents to which aromatic polymers are often susceptible.

The UHMWPE results in excellent properties such as a high abrasion resistance. high impact resistance and high melt viscosity. Hence it is used in applications where the lower molecular weight grades fail.
EXISTING KNOWLEDGE:
The synthesis of UHMWPE using conventional Zeigler Natta catalysts result in high entanglement of the chains because of the drastic reaction conditions used in such reactions. It is hence imperative that for achieving disentanglement of the polymer chains single site catalysts are needed which are highly active and exhibit living nature under milder process conditions.
The living nature of the catalyst systems is exemplified in the following patents of Fujita et al, Mitsui chemicals: US 6 875 718; EP 0 874 005; PCT Int. Appl. WO 2001005231.
Geoffrey W Coates et al have also shown the living nature of such related catalyst systems vide US 6562930; 6787624; 7119154 for the homo and copolyrnerization of propylene.
Sanjay Rastogi has also used such catalyst systems utilising its living nature to demonstrate that the UHMWPE produced was of the disentangled nature (EP 1 308 255 dated 2003). His recent US patent application 2010/0087929 demonstrates the usage of such disentangled UHMWPE for mouldable shaped parts with advantages for use in medical applications.
Teijin Aramid. NL. used such disentangled UHMWPE and developed suitable machinery to process same using solid state processing techniques followed by

drawing into tapes and fibers as exemplified in the following patent applications. WO 2009/153318, WO 2010/003971 , WO 2009/133060, WO 2009/109632, WO 2010/007062, WO 2006/136323, WO 2009/133060
WO2009127410A1 describes a method of preparation of a ultra high molecular weight polyethylene (hereinafter mentioned as "UHMWPE") of molecular weight between 1000000 g/mol and 10000000 g/mol; by using a titanium based catalyst and a co-catalyst triethylaluminium or triisobutylaluminium which has a molar ratio of magnesium compound: titanium compound lower than 3:1.
EP874005B1 deals with olefin polymerization catalysts such as a transition metal complex and organoaluminum oxy-compound as a co-catalyst and processes for
synthesi2irig polyethylene.
US5986029 deals with a process for synthesis of HDPE5 LDPE, LLDPE and copolymers of ethylene using a new catalyst transition metal complex like C5Me(CH2)2NMe2TiCl2 and its analogues and methyl alumoxane co-catalyst system.
US2003096927 deals with the synthesis of Polyethylene and its co-polymer using catalyst Bis - schiff base ligand with a cyclopentadienyl metal chloride where the metal is titanium or zirconium or hafmium and a co-catalyst methyl alumoxane.
JP2000063416 deals with the snythesis of polymers with a wide molecular weight distribution using a titanium catalyst and organoaluminumoxy compound as a co-catalyst.
CN1651472 deals with a catalyst of a IV B- family match of Schiff base containing oxyl, which has a catalytic activity for polymerising ethylene.

CN1850869 discolse a beta-ketimine vanadium alkene polymerization catalyst and the manufacture method and the application of ethylene polymerising, ethylene and norborene polymerizing, ethylene and alpha-alkene or norborene co-polymerization.
WO09091334 deals with the synthesis of self assembled catalyst which is a Li or Na salt of Schiff base made from (an aniline and di-aldehyde/ di-ketone, tri-aldehyde/ tri-ketone or tetrakis-aldehyde/tetrakis-ketone) with transition metal and a co-catalyst like organo-aluminium compound and its use for the synthesis of polyolefins of low molecular weight to ultra high molecular weight (3000 to 3000000).
US6562930 is directed to bis(salicylaldiminato)titanium complex catalysts, and highly syndiotactic polypropylene makable therewith by a chain-end control mechanism, and block copolymers containing the syndiotactic polypropylene and poly(ethylene-co-propylene) and/or poly(alpha-olefin-co-propylene), as well as to living olefin polymers and to olefin terminated to oligomers and polymers and to methods of making syndiotactic polypropylene, block copolymers and olefin-terminated oligomers and polymers from propylene.
EP1669376 relates to a dual catalyst system on the same support which is a phosphinimine ligand supported catalyst and aluminium complex with a hindered phenol as co-catalyst suitable for the polymerization of bimodal polyolefins (e.g. polyethylene) having reverse or partial reverse comonomer incorporation.
US2003060584 is directed to a process for synthesis of syndiotactic polypropylene and its block co-polymers using bis(salicylaldiminato)titanium complex and methvl alumoxane.

The state of the art discloses processes for the manufacture of polyolefins including UHMWPE. However, the UHMWPE suffers from the drawback that it can be processed only at high temperatures. Because of the high molecular weight and high melt viscosity of UHMWPE, it requires specialized processing methods like compression moulding and ram extrusion. Furthermore, processing of UHMWPE for making fibers for using in bullet proof vests involves high temperature gel spinning of polymer solutions which are energy intensive. There is a need to synthesize disentangled form of UHMWPE which can be processed at lower temperatures and can be used for a variety of purposes.The existing methods for synthesis of DUHMWPE makes use of cryogenic units for maintaining zero to sub-zero temperatures to carry out the reaction. Therefore, the synthesis of a DUHMWPE in a simple and efficient manner is a challenge. Thus, there remains a need for developing an efficient, economically viable and industrially feasible process for the synthesis of DUHMWPE.
OBJECTS OF THE INVENTION
An object of the present invention is to provide a process for synthesis of DUHMWPE under non-cryogenic conditions.
Another object of the present invention is to synthesize DUHMWPE in larger batch sizes in the existing UHMWPE facilities thereby making the process economical.
Yet another object of the present invention is to provide a process wherein, there is desired control over the reaction kinetics by optimal catalyst, co-catalyst ratio.
A further object of the present invention is to provide a process which enables a quantitative transfer of the polymer easily from the polymerization vessel by using an optimal ratio of the catalyst and co-catalyst.

Still further object of the present invention is to provide a catalyst and co-catalyst system to lower the exotherm during polymerization to maintain good morphology and control the molar mass of the polymer.
SUMMARY OF THE INVENTION
The present disclosure provides a non-cryogenic process for synthesis of DUHMWPE in a conventional UHMWPE facility using an optimal ratio of FI catalyst and co-catalyst system under relatively milder process conditions. The structure of the FI catalyst employed in the process of the present invention is as follows:

Formula I
In particular, the process of the present invention involves the following steps:
a. mixing FI catalyst of formula I with a hydrocarbon solvent containing poly-methyl aluminoxane (P-MAO) co-catalyst in a vessel under stirring before the polymerization or directly in the polymerization vessel at a temperature ranging between 25 C and 29 °C under a dry Nitrogen atmosphere; and

b. pressurizing ethylene in the polymerization vessel and polymerizing ethylene in a solution or a suspension, continuously or batch wise, in one or more stages at a temperature in the range of 30 °C to 50 °C.
Typically, the synthesis of DUHMWPE in accordance with the process of the present invention is carried in a conventional UHMWPE facilities.
Typically, the polymerization reaction is carried out in a continuous or a batch mode, preferably in a batch mode.
Typically, the ethylene pressure used for the reaction is maintained in the range of 0.3 to 50 bars.
Preferably, the range of ethylene pressure used for the polymerization reaction is between 1 to 10 bars and more specifically 1.5 bars and 2.5 bars.
Typically, the range of the optimal ratio of the co-catalyst and catalyst used in the polymerization reaction for the synthesis of DUHMWPE is in the range of 10 to 2000 and more specifically 100 to 200.
Typically, the catalyst concentration employed for the polymerization reaction ranges between 0.013 mmol of Ti and 0.021 mmol of Ti.
Typically, the hydrocarbon solvent used in the process is at least one selected from the group consisting of hexane, cyclohexane. toluene, heptane, octane, iso-octane decane. varsol and mixtures thereof.
Preferably, the hydrocarbon solvent used is varsol which is a mixture of aliphatic hydrocarbons.

Typically, the amount of hydrocarbon solvent used in the reaction ranges between 0.45 liters and 0.55 liters.
Typically, the temperature maintained for the polymerization reaction is in the rangeof43°Cto47°C.
Typically, in accordance with the process of the present invention, the agitation speed of the polymerization vessel ranges between 400 rpm and 800 rpm.
In accordance with the process of the present invention, time required for achieving a molecular weight of 5 million g/ mole of the polymer is in the range of 15 minutes to 20 minutes.
Typically, the time required for achieving molecular weight of greater than 12 million g/ mole of the polymer ranges between 55 minutes and 65 minutes.
Typically, the polymerization reaction in accordance with the process of the present invention is carried in a metal reactor.
Typically, in accordance with the process of the present invention, the yield of polymer is between 0.5 kg/g and 5.0 kg/g of catalyst, with molecular weight ranging between 0.08 and 15.0 million g/ mole of the polymer.
Typically, the bulk density of the polymer obtained in accordance with the process of the present invention ranges between 0.055 g/cm and 0.08 g/cmJ.
Typically, the crystallinity of the polymer obtained in accordance with the process of the present invention is around 90 - 95% as measured by XRD.
Typically, the particle density of the polymer obtained in accordance with the process of the present invention is up to 0.97 g/cm3.

In accordance with the present invention, there is provided DUHMWPE characterized by crystallinity of 90-95% as measured by XRD and with a particle density up to 0.97 g/cm3.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 illustrates polymerization kinetics monitored over time for achieving optimum catalyst concentration for the polymerization reaction for examples 1-11 mentioned in Table 1
Figure 2 illustrates polymerization reaction kinetic profile in 1 L SS316 metal Buchi reactor dealing with control of the polymerization exotherm below 45 C monitored over time for examples 12-14 mentioned in Table 2.
Figure 3 illustrates polymerization exotherm dealing with quenching of polymerization exotherm in a metal reactor Buchi, SS316 from a temperature range of 50°C - 55 C to 40 C - 45 C in comparison to the glass reactor for examples 15-26 mentioned in Table 3.
DETAILED DESCRIPTION OF THE INVENTION
In accordance with the present invention, there is provided a non-cryogenic process for synthesis of DUHMWPE in a conventional UHMWPE facility using an optimal ratio of Fl catalyst and co-catalyst system under relatively milder process conditions.

The process of the present invention comprises the following steps:
a. mixing FI catalyst of formula I with a hydrocarbon solvent containing poly-
methyl aluminoxane (P-MAO) co-catalyst in a vessel under stirring before the
polymerization or directly in the polymerization vessel at a temperature ranging
between 25 C and 29 C under a dry Nitrogen atmosphere; and
b. pressurizing ethylene in a polymerization vessel and polymerizing ethylene in a
solution or a suspension, continuously or batch wise, in one or more stages at a
temperature in the range of 30 °C to 50 °C.
Preferably, the temperature range is in the range of 43 °C to 47 °C and still preferably, the temperature range is between 44 °C and 45 °C.
In accordance with one of the embodiments of the present invention, the ethylene pressure used for the polymerization reaction is in the range of 0.3 bars and 50 bars.
Preferably, the range of ethylene pressure used for the polymerization reaction is between I to 10 bars and more specifically 1.5 bars and 2.5 bars.
The molar mass of the polymer is regulated by controlling the kinetics of the polymerization taking advantage of the living characteristics of the catalyst.
Typically, in accordance with the process of the present invention, the agitation speed of the polymerization vessel is maintained between 400 and 800 rpm.
Preferably, the agitation speed of the polymerization vessel is maintained between 500 rpm and 700 rpm and still preferably between 500 rpm and 600 rpm.

In accordance with another aspect of the present invention, there is provided a Jiving polymerization system comprising FI catalyst of formula I and poly-methyl aluminoxane (P-MAO) co-catalyst system.
The living polymerization system employed in the present invention results in synthesis of DUHMWPE of desired molecular weight. The molecular weight of DUHMWPE synthesized in accordance with the present invention varies according with the time for which the reaction is carried out.
Typically, the preferred time for achieving a molecular weight of 5 million g/mole is between 15 minutes and 20 minutes.
Preferably, the time is between 16 minutes and 18 minutes and still preferably, around 17 minutes.
In accordance with one of the embodiments of the present invention, the time required for achieving molecular weight of greater than 12 million g/ mole of the polymer ranges between 55 minutes and 65 minutes.
In accordance with the present invention, the solvent employed for the polymerization reaction is a hydrocarbon solvent.
The hydrocarbon solvent used for the reaction facilitates efficient removal of heat combined with enhanced operational safety. Furthermore, it also keeps the polymer formed in suspension, allowing it to settle down quickly facilitating ease of removal from the vessel. Polymerization reaction carried out in other solvents results in the floating of the polymer.
Typically the hydrocarbon solvent is at least one selected from the group consisting of hexane. cyclohexane, toluene, heptane, octane, iso-octane, decane, varsol and mixtures thereof.

Preferably, the hydrocarbon solvent used is varsol which is a mixture of aliphatic hydrocarbons.
Typically, the amount of hydrocarbon solvent used in the reaction ranges between 0.45 liters and 0.55 liters.
In accordance with the present invention, an optimal ratio of the co-catalyst and catalyst is used in the polymerization reaction for the synthesis of DUHMWPE.
Typically, the co-catalyst/catalyst molar ratio used for the polymerization reaction is in the range of 10 to 2000 and more specifically 100 to 200.
Typically, the catalyst concentration employed for the polymerization reaction ranges between 0.013 mmol of Ti and 0.021 mmol of Ti.
Preferably, the catalyst concentration used in the process of the present invention ranges between 0.016 mmol of Ti and 0.017 mmol of Ti.
In accordance with the present invention, the polymerization reaction is carried out in a continuous or a batch mode.
Typically, the polymerization reaction in accordance with the process of the present invention is carried out in a batch mode.
In accordance with one of the embodiments of the present invention, the polymerization vessel used for the synthesis of DUHMWPE is a metal reactor like Buchi, SS316 to quench the heat of polymerization.
Typically, in accordance with the process of the present invention, the yield of polymer is between 0.5 kg/g and 5.0 kg/g of catalyst, with molecular weight ranging between 0.08 and 15.0 million g/ mole of the polymer.

Typically, the bulk density of the polymer obtained i.n accordance with the process of the present invention is between 0.055 g/cc and 0.08 g/cc.
Typically, the crystallinity of the polymer obtained in accordance with the process of the present invention is around 90 - 95% as measured by XRD with particle density up to 0.97 g/cm3.
The present invention will now be described with the help of following non-limiting examples.
Examples
1) Optimum catalyst concentration under the operating conditions
A 1.0 dm3 reactor was charged with 500 cm3 of varsol containing requisite amount of P-MAO and the catalyst resulting in a molar ratio of about 100 to 200. The initial reactor temperature was around 25 °C and kept agitated at 500 rpm. The reactor was then pressurized with 2 bar of ethylene and maintained at same pressure to replenish the ethylene consumed. The polymerization kinetics was monitored over time. The respective individual temperature profiles can be seen in Fig 1. These examples were aimed to arrive at the optimum catalyst concentration under the operating conditions so that the polymerization exotherm did not cross 45 °C preventing fusion of the individual polymer molecules. The experiments also served to freeze the duration of polymerization for achieving the desired molecular weight. Conventional experiments which serve as comparison are normally carried out at a temperature of 0 °C to -10 °C at atmospheric pressure of ethylene and thus the rate is abysmally slow; making the process of present invention much superior as regards product economics, without sacrificing on the polymer characteristics, like molecular weight, morphology and bulk density.

Example 5 was deliberately carried out at ethylene pressure of 1 bar to visualize the drop in rate.
The results of the polymerization are shown below in Table 1.
TABLE 1 Polymerization experiments using 1.0 dm reactor (Buchi glasuster polyclave). 0.5 dm3 of varsol, 2 bar of ethylene (d), 500 rpm agitation, P-MAO/catalyst molar ratio 150.
Table 1

Exp.No. 1 2 J 4 5 6 7 8 9 10 11
Cat cone. (mg) 14 14 14 14 14 14 10.5 7 10.5 10.5 10.6
Time
(min) 20 15 10 15 15 15 15 15 15 15 15
Yield (g) 35 30 27 30 23 29 24.5 5 24 24 21
Yield (g/g of cat) 2500 2143 1929 2143 1643 2071 2333 714 2286 2286 2000
Yield
(g/mmol
ofTi) 2008 1722 1549 1722 1320 1664 1875 574 1836 1836 1607
RSV
(df/g) ASTM-D4020 30.4 28.4 20.3 27.7 31.1 25 27.4 26 28.8 28.4 27.7
MW
(Millions) ASTM-D4020 5.7 5.3 3.3 5.1 5.9 4.4 5.0 4.7 5.4 5.3 5.1

2) Controlled polymerization exotherm below 45°C
A 1.0 dm3 metal reactor (Buchi, SS316) was charged with 500 cm3 of varsol containing requisite amount of P-MAO and the catalyst resulting in a molar ratio of about 100 to 200. The initial reactor temperature was around 25 °C and kept agitated at 500 rpm. The reactor was then pressurized with 2 bar of ethylene and maintained at same pressure to replenish the ethylene consumed. The polymerization kinetics was monitored over time. The respective individual temperature profiles can be seen in Fig. 2. These examples were aimed to illustrate how the polymerization exotherm could be controlled below 45 °C under more or less identical process conditions due to effective heat removal in a metal reactor thus preventing fusion of the individual polymer molecules. The experiments also served to freeze the duration of polymerization for achieving the desired molecular weight. Conventional experiments which serve as comparison are normally carried out at a temperature of 0 °C to -10 °C at atmospheric pressure of ethylene and thus the rate is abysmally slow; making the process of present invention much superior as regards product economics, without sacrificing on the polymer characteristics, like molecular weight, morphology and bulk density.
The results of the polymerization are shown below in Table 2.
Table 2. Polymerization experiments using 1.0 dm3 SS316 metal Buchi reactor, 0.5 dm3 of varsol, 2 bar of ethylene (C2). 500 rpm agitation., P-MAO/catalyst molar ratio 150.
Table 2 SS316 1L metal reactor (Buchi)

Exp.No. 12 13 14
Cat cone, (mg) 13 13 13
Time (min) 18 15 17
Yield (g) 32 28 30
Yield {gig of cat) 2406 2154 2273
Yield (g/mmol ofTi) 1933 1730 1826
RSV
(dl/g) ASTM-
D4020 28.8 27.7 28.4
MW (Millions) ASTM-D4020 5.4 5.1 5.3
3) Polymerization reaction in SS316 metal Buchi reactor
Examples 15 to 19 have been performed in a Buchi glass reactor and the catalyst concentrations in examples 18 and 19 have been reduced to lower the exotherm during polymerization as can be seen in Fig 3. Examples 20 to 26 have been performed in a SS316 metal Buchi reactor of capacities 1.0 dm , 2.0 dmJ and 5.0 dmJ with proportionate increase of the catalyst, co-catalyst and polymerization medium. The results in Table 3 and Fig 3 clearly illustrate how the polymerization exotherm has been quenched from a temperature range between 50 C - 55 C to 40 °C - 45 °C in comparison to the glass reactor. This also resulted in improved . polymer morphology. The reactors were charged with requisite amount of varsol containing requisite amount of P-MAO and the catalyst resulting in a molar ratio of about 100 to 200. The initial reactor temperature was around 25 °C and kept agitated at 500 rpm. The reactor was then pressurized with 2 bar of ethylene and maintained at same pressure to replenish the ethylene consumed. The polymerization kinetics was monitored over time. The respective individual temperature profiles can be seen in Fig 3. These examples were aimed to illustrate

the difference between the MOC of the reactor during polymerization scale up process and how the polymerization exotherm could be controlled below 45 °C under more or less identical process conditions due to effective heat removal in a metal reactor thus preventing fusion of the individual polymer molecules. The experiments also served to check the R&R of the polymerization for achieving the desired molecular weight. Conventional experiments which serve as comparison are normally carried out at a temperature of 0 °C to -10 °C at atmospheric pressure of ethylene and thus the rate is abysmally slow; making the process of present invention much superior as regards product economics, without sacrificing on the polymer characteristics, like molecular wdght, morphology and bulk density.
The results of the polymerization are shown below in Table 3. RSV and Molecular weight are based on ASTM-D4020.
Table 3

Exp.No. 15 16 17 18 19 20 21 22 23 24 25 26
Cat
concn 14 14 14 10.5 10.5 13 13 13 26 26 65 65
(mg)
Time, min 15 15 15 15 15 18 15 15 15 15 15 15
Yield, g 30 30 29 24.5 24 32 28 30 56 57 107 102
Yield,
g/gof cat 2143 2143 2071 2333 2286 2406 2154 2273 2154 2192 1574 1500
Yield,
g/mmol
of Ti 1722 1722 1664 1875 1836 1933 1730 1826 1730 1761 1264 1205
RSV, dl/g 28.4 27.7 27.4 27.4 28.8 28.8 27.7 28.4 25 25.7 27 27.4
MW, M 5.3 5.1 5.0 5.0 5.4 5.4 5.1 5.3 4.4 4.6 4.9 5.0

4) Molecular weight of the polymer increases with time
Table 4 provides polymerization experiments performed under different conditions for illustration. The bulk density of the polymer obtained was between 0.055 to 0.08 g/cc. Molecular weight obtained was over a wide range to suit the requirement. Providing more time resulted in molecular weight greater than 12 M g /mole since the phenomenon was of a living nature. RSV and molecular weight were based on ASTM D-4020.
Table 4

Exp.No. 27 28 29 30 31 32 33
Cat. Concn.(mg) 220 14 11 11 11 12 14
Time, min 90 20 60 10 60 15 60
Reactor 19 L,
SS316 IL,
glass IL,
glass IL,
glass IL,
glass 1 L, glass 1 L, glass
P-MAO/catalyst (molar ratio) 1844 175 220 204 204 218 204
Medium Varsol hexane Toluene Varsol Varsol Varsol Varsol
Polymerization temperature °C 40±1°
c 38±1° C 37±1°C 42±1° C 32±r c 49±1°C 34±1°C
Ethylene pressure, bars 2 2 1 1 0.3 2 (containing 0.2 bar H2) 2
Yield, g 1050 33 17 14.5 7 19.8 58
Yield, g/g of cat 4773 2357 1545 1318 636 1650 4143
Yield, g/mmol of Ti 3834 1894 1242 1059 511 1326 3328
RSV, dl/g 48 35.8 41.8 19.6 15.5 1.35 52
MW,M 10.8 7.2 8.9 3.1 2.3 0.08 12.1

5) Scale up of the polymerization reaction
Polymerization experiments were also performed in a 19.0 dm3 SS316 metal Buchi reactor with proportionate quantity of varsol. 2 bar of ethylene (C2), 500 rpm agitation, P-MAO/catalyst molar ratio 150 to 200 as part of scale up of the process. The productivity was closer and some what better than the 5.0 dm reactor and the polymer characteristics like morphology, molecular weight, crystallinity. bulk density etc were comparable. Trials in a 90 dm reactor were also comparable and resulted in 2 Kg of the material, a substantial quantity physically since the bulk density of the product was only around 0.055 to 0.08 g/cmJ.
ANALYSIS OF THE POLYMER PRODUCT OF THE PRESENT INVENTION
The crystallinity of the polymer as measured by XRD was around 90 - 95% and the particle density was up to 0.97 g/cm .
Routine tests for the disentangled nature of the polymer chains through analysis like DSC and RDA conclusively establish the material to be disentangled ultra high molecular weight polyethylene, which has been synthesized on such a large scale with highly improved process economics for the first time.
POLYMERIZATION PROCESS VALIDATION
The process was validated in a 2KTA plant which was producing normal UHMWPE using a Ti supported on MgCl2 Ziegler-Natta catalyst.

TECHNICAL ADVANCEMENT:
The process for synthesis of DUHMWPE as described in the present invention has several advantages which include:
• unlike the routinely practised process carried out at zero to sub zero temperature, the synthesis of DUHMWPE in accordance with the present invention is carried out at a temperature ranging between 30 °C and 50 °C.
• the synthesis of DUHMWPE in accordance with the process of the present invention is carried out in a conventional UHMWPE facility thereby obviating the need for a specialized polymerization vessel for carrying out the reaction.
• unlike the other reactions reported in the prior art, the process of the present invention does not end up in a messy reactor since it provides an optimal ratio of the co-catalyst/catalyst ranging between 100 to 200 for carrying out the polymerization reaction resulting in quantitative transfer of the polymer easily from the polymerization vessel.
• the synthesis of DUHMWPE in accordance with the process of the present invention is faster and it also results in a polymer with good morphology.
• the synthesis of DUHMWPE in accordance with the present invention is carried in a metal reactor resulting in effective heat removal. Furthermore, individual polymer molecules do not get fused with each other during the process of the present invention.

• the synthesis of DUHMWPE in accordance with the present invention is
simple, safe and cost-effective.
While certain embodiments have been described, tnese embodiments have been presented by way of example only, and are not intended to limit the scope of the invention. Variations or modifications to the design and construction of this invention, within the scope of the invention, may occur to those skilled in the art upon reviewing the disclosure herein. Such variations or modifications are well within the spirit of this invention. The accompanying claims and their equivalents are intended to cover such forms and modifications as would fall within the scope and spirit of the invention.
The numerical values mentioned for the various physical parameters, dimensions or quantities are only approximations and it is envisaged that the values higher/lower than the numerical values assigned to the parameters, dimensions or quantities fall within the scope of the invention, unless there is a statement in the specification specific to the contrary.

We claim:
1. A non-cryogenic process for synthesis of disentangled ultra high molecular weight polyethylene (DUHMWPE) comprising the following steps:
a. mixing FI catalyst of formula I

Formula I
with a hydrocarbon solvent containing poly-methyl aluminoxane (P-MAO) co-catalyst in a vessel under stirring before polymerization or directly in the polymerization vessel at a temperature ranging between 25 °C and 29 °C under a dry Nitrogen atmosphere; and
b. pressurizing ethylene in the polymerization vessel and polymerizing ethylene in a solution or a suspension, continuously or batch wise, in one or more stages at a temperature in the range of 30 °C to 50 °C.
2. A process as claimed in claim 1, wherein the synthesis of DUHMWPE is carried in a conventional UHMWPE production facilities.

3. A process as claimed in claim 1. wherein the pressure of ethylene is in the range of 0.3 bars to 50 bars.
4. A process as claimed in claim 1, wherein the pressure of ethylene ranges between 1.5 bars and 2.5 bars.
5. A process as claimed in claim 1, wherein the molar ratio of co-catalyst/catalyst is in the range of 100 to 200.
6. A process as claimed in claim 1, wherein the catalyst concentration employed for the polymerization reaction ranges between 0.013 mmol of Ti and 0.021 mmol ofTi.
7. A process as claimed in claim 1. wherein the temperature maintained for the polymerization reaction is in the range of 30 °C to 50 °C.
8. A process as claimed in claim 1, wherein the temperature maintained for the polymerization reaction is in the range of 43 °C to 47 °C.

9. A process as claimed in claim 1, wherein the agitation speed of the polymerization vessel ranges between 400 rpm and 800 rpm.
10. A process as claimed in claim 1, wherein the time required for achieving a molecular weight of 5 million g/ mole of the polymer is in the range of 15 minutes to 20 minutes.
11. A process as claimed in claim 1, wherein the time required for achieving molecular weight of greater than 12 million g/ mole of the polymer ranges between 55 minutes and 65 minutes.

12. A process as claimed in claim 1, wherein the hydrocarbon solvent is at least one selected from the group consisting of hexane, cyclohexane, toluene, heptane, octane, iso-octane, decane, varsol and mixtures thereof.
13. A process as claimed in claim 1. wherein the hydrocarbon solvent used is varsol.
14. A process as claimed in claim 1, wherein the amount of the hydrocarbon solvent used in the reaction ranges between 0.45 liters and 0.55 liters.

15. A process as claimed in claim 1, wherein the polymerization reaction is carried out in a continuous or a batch mode.
16. A process as claimed in claim 1, wherein the polymerization reaction is carried out in a batch mode.
17. A process as claimed in claim 1, wherein the polymerization reaction is
carried out in a metal reactor.
18. A process as claimed in claim 1, wherein the yield of the polymer obtained is
between 0.5 kg/g and 5.0 kg/g of catalyst.
19. A process as claimed in claim 1. wherein the molecular weight of the polymer obtained is ranging between 0.08 and 15.0 million g/ mole of the polymer.
20. A process as claimed in claim 1, wherein the bulk density of the polymer
■J -7
obtained is between 0.055 g/cmJ and 0.08 g/crn3.
21. A process as claimed in claim 1, wherein the crystallinity of the polymer
obtained as measured by XRD is around 90 - 95%.

22. A process as claimed in claim I, wherein the particle density of the polymer obtained is up to 0.97 g/cm3
23. A DUHMWPE synthesized by the process as claimed in claim 1, characterized by crystaJlinity of 90-95% as measured by XRD and with a particle density up to 0.97 g/cm3.