Title of Invention

"A PROCESS TO PRODUCE HIGH VISCOSITY PAOS BASED ON 1-DECENE/1- DODECENE"

Abstract A process for producing a polyalphaolefin (PAO) comprising contacting a feed comprising an olefin mixture, the olefin mixture consisting of 40 to 60% 1-decene monomer units and 60 to 40% 1-dodecene monomer units, on a molar basis, with an oligomerization catalyst, the oligomerization catalyst being an aluminum halide complexed with water, and optionally a diluent, in an oligomerization reaction zone under oligomerization conditions for a time sufficient to produce a PAO having a viscosity of from about 40 cSt to about 100 cSt at 100°C (ASTM D445), and a number average molecular weight of from about 1200 to about 40001 and optionally distilling and hydrogenating the PAO.
Full Text HIGH VISCOSITY PAOS BASED ON 1-DECENE/l-DODECENE
FIELD OF THE INVENTION
[0001] This invention relates to the use of 1-decene/l-dodecene olefin mixtures to produce high viscosity polyalphaolefins (PAOs). The products are particularly useful as lubricant base stocks.
BACKGROUND OF THE INVENTION
[0002] PAOs comprise a class of hydrocarbon lubricants which has achieved importance in the lubricating oil market. These materials are typically produced by the catalytic oligomerization (polymerization to low-molecular-weight products) of α-olefins typically ranging from 1-octene to 1-dodecene, with 1-decene being a preferred material, although polymers of lower olefins such as ethylene and propylene may also be used, including copolymers of ethylene with higher olefins, as described in U.S. Patent No. 4,956,122 and the patents referred to therein. PAO products may be obtained with a wide range of viscosities varying from highly mobile, fluids of about 2 cSt at 100° C to higher molecular-weight, viscous materials which have viscosities exceeding 100 cSt at 100° C. [0003] The PAO's are typically produced by the polymerization of olefin feed in the presence of a catalyst such as AlCl3 or BF3. Processes for the production of PAO lubricants are disclosed in numerous patents, for example, U.S. Patent Nos. 3,149,178; 3,382,291; 3,742,082; 3,780,128; 4,172,855 and 4,956,122. [0004] High viscosity PAOs (defined herein as PAOs having a kinematic viscosity at 100°C of >20 cSt as measured by ASTM D 445) are normally produced via cationic oligomerization of linear alpha olefins. 1-decene is the preferred olefin for oligomerization. PAOs have also been produced using mixtures of olefins containing 1-octene and 1-dodecene.
[0005] High viscosity PAOs produced via A1C13 catalyzed olefin oligomerization have been available commercially for many years, e.g., from ExxonMobil Chemical Company. These PAOs are produced either from 1-decene, or from a mixture of 1-octene/1-dodecene. When oligomerizing olefin mixtures, the composition needs to be carefully controlled to produce PAOs with
the desired blend of low temperature properties including pour point, viscosity,
and appearance. Typically, use of olefins with molecular weight greater than 1-
decene results in PAOs with high pour points. As a result, when oligomerizing
olefin mixtures, a combination of low and high molecular weight olefins (with
respect to 1 -decene) is generally used.
[0006] U.S. 4,533,782 is directed to polymerizing cationically polymerizable
monomers including C3-C14 linear or branched 1-olefins using a catalyst
comprising an aluminum compound of the formula RnAlX3-n and a compound
having the formula R'X (X being a halide in both formulas) in solution.
[0007] U.S. Patent No. 5,196,635 discloses the use of a catalyst prepared by
reacting in an organic solvent an aluminum halide and a proton donor useful in
oligomerizing C6 to C20 straight chain alpha olefins.
[0008] U.S. Patent No. 6,646,174 teaches a process for oliogmerization of 1-
dodecene and 1-decene to produce a PAO product having a kinematic viscosity in
the range of from about 4 to about 6 cSt at 100°C and a viscosity index of 130 to
145, and a pour point of-60°C to -50°C.
[0009] U.S. Patent No. 6,686,511 directed to a process for making a lube base
stock having at least four steps, including separation of an olefinic feedstock in a
first separator into fractions and contacting a light olefin fraction with a first
oligomerization catalyst in a first oligomerization zone to produce a first product,
which is subsequently contacted with a medium olefin fraction and an
oligomerization catalyst in a second oligomerization zone to produce a second
product.
[0010] U.S. Patent No. 6,395,948 discloses the use of an acidic ionic liquid
oligomerization catalyst, described by the general formula Q+A-, for the
preparation of high viscosity PAOs from decene or dodecene in the absence of an
organic diluent. See also U.S. Application Nos. 2002/0128532 and
2004/0030075.
[0011] JP1095108 is directed .to a method for manufacturing an olefin
oligomer using a Lewis acid and an alkyl cyclohexane.
[0012] RU2212936 is directed to a cationic oligomerization of olefins that
uses a catalyst containing active aluminum and a co-catalyst that is an
organohalide compound RX, where R is a primary, secondary, or tertiary alkyl,
allyl, benzyl, acetyl or benzoyl and X is chlorine, bromine or iodine.
[0013] Additional patents of interest include WO 99/38938 and U.S. Patent
Nos. 6,706,828 and 6,713,582.
[0014] Current practice does not provide enough flexibility in the choice of
feed olefin/olefin mixtures that can lead to an economic method of achieving a
high viscosity PAO composition having adequate low temperature performance
suitable for end use applications such as industrial lubricants.
[0015] The present inventors have surprisingly discovered a method of
producing high viscosity PAOs having excellent low temperature performance
from 1-decene/l-dodecene mixtures.
SUMMARY OF INVENTION
[0016] The present inventors have discovered 1-decene/l-dodecene mixtures that can be oligomerized to high viscosity PAOs which may be characterized by a kinematic viscosity of from about 40 to about 100 cSt at 100 °C (ASTM D-445), and in an embodiment possess desired low temperature properties, such as low pour point.
[0017] In an embodiment, the process introduces the mixture of olefins with a catalyst into a first reactor to produce a partially reacted product that is fed into a second reactor to complete the reaction. In yet another embodiment, the process uses 3-reactors in series to complete the reaction.
[0018] In another embodiment, the process produces a 40 cSt PAO at 100 °C in the absence of a solvent and in still another embodiment, the process produces a 100 cSt PAO at 100 °C using a solvent. In yet another embodiment, the high viscosity PAOs of the present invention have a number average molecular weight of between about 1200 to about 4000.
[0019] These and other embodiments, objects, features, and advantages will become apparent as reference is made to the following drawings, detailed description, examples, and appended claims.
DETAILED DESCRIPTION
[0020] The invention is directed to mixtures of linear alpha olefins comprising decene and 1-dodecene oligomerized using an aluminum halide complex with water to produce high viscosity PAOs having, in an embodiment, a kinematic viscosity of from about 40 and about 100 cSt at 100 °C (ASTM D-445) and which in an embodiment possess the desired low temperature properties, such as low pour point.
[0021] The process according to the invention comprises co-feeding a mixture of linear alpha olefins (LAO) comprising 1-decene and 1-dodecene concurrently with the catalyst. The catalyst may be any known catalyst for the polymerization of LAOs to PAOs, such as AlCl3. Preferably, the catalyst is a complex comprising a proton donor such as water with an aluminum halide, preferably aluminum trichloride - water complex having 0.5 moles of water per mole of aluminum chloride. The reaction may be batch, semi-batch or continuous, in a single or multi-stage reactors. In a preferred embodiment, the mixture of catalyst and linear alpha olefins (LAOs) is preferably fed into a first oligomerization reactor where it is partially reacted and then into a second oligomerization reactor where the reaction may be allowed to continue to completion or where the reaction may be allowed to proceed further and then the mixture of catalyst, linear alpha olefins and oligomers are fed into a third oligomerization reactor where the reaction is completed. Additional oligomerization reactors may be used in series. [0022] The reaction zone may be any reaction means known in the art that provides for the reaction under suitable conditions maintained and controlled so as to provide for the production of oligomers of the LAO feed. The LAO feed comprising a mixture of 1-decene and 1-dodecene and catalyst may be introduced either separately or together into the first reaction zone. It is preferred that the reactors each be equipped with a mixing or stirring means for mixing the feed and catalyst to provide intimate contact. In a more preferred embodiment, continuous stirred tank reactors (CSTRs) are used in series. CSTRs are per se known in the art. Also in a preferred embodiment, no recycle of unconverted monomer is used. [0023] An effective amount of catalyst is provided. One of ordinary skill in the art in possession of the present disclosure can determine an effective amount
without undue experimentation. In a preferred embodiment, the catalyst concentration is between 0.5 to 4 wt.% of the total reaction mass (e.g., monomers, catalyst, diluent and/or other optional ingredients). It is known in the art that the addition of aromatics in small amounts improves the oligomerization of LAOs. In the 100 cSt examples below, 0.5 wt. % xylenes was present in the feed.
[0024] Reaction conditions are such as to cause effective conversion of monomers to the desired product. Such conditions may also be determined by one of ordinary skill in the art in possession of the present disclosure without undue experimentation. In a preferred embodiment, the reactor temperatures are between about 80 and HOT (between about 26 and 60°C) and residence time of about 1.5 to about 3 hours in reactor one and about 0.5 to about 1.5 hours in reactor 2, if used. The residence time in a third reactor, if used would typically be from about 10 minutes to about 1 hour. The reaction is not particularly pressure-dependent and it is most economical to operate the reactors at a low pressure, preferably from about atmospheric to about 50 psia.
[0025] In an embodiment, no solvent is used. In another embodiment, an inert diluent may be used, preferably selected from fluids such as C5-C19 paraffinic hydrocarbons, preferably a C6-C13 paraffinic fluid such as Norpar™ 12 fluid, an aliphatic (paraffinic) solvent having primarily twelve carbon aliphatic compounds, available from ExxonMobil Chemical Company, Baytown, TX.
[0026] The product of the reaction typically comprises C20-24 dimers, C30-36 trimers, C40-48 tetramers, C50-60 pentamers, and C60+ heavies.
[0027] The reaction mixture is then distilled to remove unreacted monomeric and dimeric species. In a preferred embodiment, the resulting product is typically hydrogenated to saturate the oligomers to provide a product having a desired viscosity, for example 40 cSt or 100 cSt at 100 °C.
[0028] Experimental
[0029] The following examples are meant to illustrate the present invention and provide a comparison with other methods and the products produced therefrom. Numerous modifications and variations are possible and it is to be
understood that within the scope of the appended claims, the invention may be practiced otherwise than as specifically described herein.
[0030] The reactions were carried out in a three-neck 5-liter round bottom jacketed glass flask (reactor) that was fitted with a motor driven stirrer and a baffle. A pump Circulated chilled water through the jacket to control reaction temperature. About two thousand grams of the LAO feed were charged into a feed burette. In the case of 100 cSt PAO, Norpar® 12 Fluid was also added to the olefin mixture (25-30 wt. % of olefins) to improve mixing and heat transfer during oligomerization. No diluent was added in the case of the 40 cSt PAO. A pump was used to feed the LAO into the reactor at a controlled rate. The reactor was dried and purged with dry nitrogen to remove moisture before the start of oligomerization. The reactor was continuously purged with small amount of nitrogen during the reaction as well. The desired amount of AlCl3 catalyst, 0.8 to 4.0 wt. % of feed, was pre-weighed and stored in closed glass vials. The AlC3 is commercially available from numerous sources. The AlCl3 used below was purchased from Gulbrandsen Chemicals. Other cationic oligomerization catalysts such as AlBr3 will also be efficient according to the present investigation. In the case of AlCl3, the present inventors have found that less catalyst is necessary using finer granularity catalyst.
[0031] At the start of oligomerization, feed olefin mixture was pumped into the flask for 15 minutes under vigorous agitation, and with cooling water flowing through the jacket. The AlCl3 catalyst from a glass vial was emptied into the reactor next, and a measured amount of DI (deionized) water was injected into the flask via a long needle syringe. The amount of DI water injected corresponded to 0.5 moles of water/mole of AlCl3. The feed was added continuously over a period of two to five hours into the reactor. The required amounts of catalyst and DI water were added at the intervals of 15 minutes. The oligomerization reaction was allowed to proceed additional one to three hours after the olefin and catalyst additions were completed. The reaction temperature ranged between 30 °C to 60 °C.
[0032] The reaction was quenched by adding the reactor contents into an equal volume of caustic (5 wt. % aqueous sodium hydroxide) solution at 65-70°C.
The quenched mass was subsequently washed two times with hot water at 65-
70°C. The viscous oil was next separated from the aqueous layer and distilled to
remove water, unconverted monomer and dimer (and solvent if present). A
material balance on the distillation indicated a feed olefin conversion of 98-99%.
The viscous oil was de-chlorinated thermally and hydrogenated over Pd catalyst.
[0033] For each of the reported examples below, 100°C and 40°C Kinematic
Viscosity was measured according to ASTM D-445 at the respective
temperatures; Pour Point was determined according to ASTM D-97; and Viscosity
Index (VI) was determined according to ASTM D-2270. Number average
molecular weight (Mn) was measured by Gel Permeation Chromatography using a
Waters 150 gel permeation chromatograph equipped with a differential refractive
index (DRI) detector. The numerical analyses were performed using the
commercially available standard Gel Permeation chromatography software
package.
[0034] The following examples are directed to the making of a 40 cSt PAO
and comparisons..
[0035] Examples 1 & 2.
[0036] The physical property data for commercial PAOs produced with
conventional olefin feed (1-decene for Example 1 and 1-octene/l-dodecene for
Example 2) is shown as Examples 1 and 2 in Table 1, below. A pour point of -42
°C is obtained for the product. The Viscosity Index, VI, of the product ranges
between 150 to 151.
[0037] Examples.
[0038] The oligomerization of a 55/45 wt. % mixture of C10/C12 olefins (1-
decene and 1-dodecene) was carried out using 1.45 wt. % AlCl3 concentration by
the procedure described above. The olefin addition time was 2 hours (add time)
while the reaction mass was held (hold time) for an additional hour. The
temperature varied between 45 °C to 61 °C during course of reaction. This resulted
in a PAO product with a pour point of-42 °C and a VI of 152.
[0039] Example 4.
[0040] The procedure was the same as in Example 3 except that the feed
composition was 50/50 wt. % mixture of the C10/C12 olefins, the catalyst
concentration was 1.33 wt. % AlCl3. The reaction temperature varied between
45°C to 58 °C. The pour point of the product was -42 °C and the VI was 151.
[0041] Example 5.
[0042] The procedure was the same as Example 3 except that the feed
composition was 100% C12 olefin. The add time was 3 hours, the hold time was 1
hour and the catalyst concentration was 1.3 wt. % AlCl3. The reaction
temperature ranged between 45 to 50°C. The pour point of the product was -33°C
and the VI was 158.
[0043] Example 6
[0044] The procedure was the same as Example 3 except that the feed
composition was 50/50 wt. % mixture of the C10/C12 olefins. The add time was 3
hours, the hold time was 1 hour, the catalyst concentration was 1.4 wt. % and the
reaction temperature varied between 45 to 50 °C. The pour point of the product
was -21 °C and the VI was 161.
[0045] The results of the above examples are shown in Table 1, below. It is
apparent that a carefully controlled composition of C10/C12 olefins is needed to
produce a 40 cSt PAO with desired low pour point.
[0046] Table 1

(Table Removed)
[0047] The following examples are directed to the making of 100 cSt PAO
and comparisons.
[0048] Examples 7 & 8.
[0049] The physical property data for commercial PAOs produced with
conventional olefin feed (1-decene for Example 7 and 1-octene/l-dodecene for
Example 8) is shown as Examples 7 and 8 in Table 2 below. A pour point of-33
°C is obtained for the product. The Viscosity Index, VI, of the product is 168.
[0050] Example 9.
[0051] The oligomerization of a 55/45 wt. % mixture of the C10/C12 olefins in
laboratory was carried out using 2.45 wt. % AlCl3 concentration by the procedure
described in the experimental section. The feed add time was three hours while the
hold time was two hours. The reaction temperature varied between 37 °C to 45 °C.
The product PAO had a pour point of-33 °C while the VI was 173.
[0052] Example 10.
[0053] Same as Example 9 except that the feed was a 50/50wt. % mixture of
the C10/C12 olefins, the catalyst concentration was 3.0 wt. % AlCl3 and the
reaction temperature ranged between 37 °C to 45 °C. The product had a pour point
of -33 °C while the VI was 173.
[0054] Example 11.
[0055] Same as example 9 except that the feed was 100 wt. % C12 olefin. The
add time was three hours, the catalyst concentration was 3 wt. % AlCl3 and the
reaction temperature was 40 to 45 °C. The product had a pour point of -27 °C and
a VI of 176.
[0056] Example 12.
[0057] The pour point increased to -21 °C when a 60/40 (wt. %) mixture of
C12/C14 olefins was used. The oligomerization procedure was the same as in
Example 9. The add time was 3 hours, the hold time was 2 hours, and the catalyst
concentration was 2.8 wt. %. The product had a VI of 180.
[0058] The results of the above examples are shown in Table 2, below. It is
apparent that a carefully controlled composition of C10/C12 olefins is needed to
produce a 100 cSt PAO with desired low pour point. It is also observed that a 100
cSt PAO with desirable low pour point can not be produced by this technology
with olefins or olefin mixtures having carbon number greater than 12.
[0059] Table 2

(Table Removed)
[0060] Example 13
[0061] The oligomerization of a 55/45 wt. % mixture of the C10/C12 olefins in a 2-CSTR commercial set-up was carried out to produce a 40 cSt PAO. The process used an AlCl3 concentration of 1.2 wt. %, a reaction temperature of 50°C, 0.5 mols of water per mole of AlCl3, and a residence time of 2 hr and 1 hr in reactors 1 and 2 respectively. The product PAO had a 100°C viscosity of 40.19 cSt, a VI of 152 and a pour point of -51 °C. [0062] Example 14
[0063] The same 2-CSTR set-up was also used to produce a 100 cSt PAO using a 55/45 wt. % mixture of the C10/C12 olefins. The concentration of AlCl3 was 3.0 wt. %, 0.5 mols of water were used per mole of AlCl3, the reaction temperature was 40 °C, the concentration of the diluent (Norpar™12) was 22 wt. % and the residence time in reactors 1 and 2 were 2.5 hr and 1.2 hr respectively. The product PAO had a 100 °C viscosity of 104.2 cSt, a VI of 172 and a pour point of-39 °C.
[0064] While the illustrative embodiments of the invention have been described with particularity, it will be understood that various other modifications will be apparent to and can be readily made by those skilled in the art without departing from the spirit and scope of the invention. Accordingly, it is not intended that the scope of the claims appended hereto be limited to the examples. Rather, many variations will suggest themselves to those skilled in this art in light of the above detailed description. All such obvious variations are within the full intended scope of the appended claims. Preferred embodiments of the present invention include: a process for producing a polyalphaolefin (PAO) comprising contacting a feed comprising 1-decene and 1-dodecene with an oligomerization catalyst in an oligomerization reaction zone under oligomerization conditions for a time sufficient to produce a PAO having a viscosity of from about 40 cSt to about 100 cSt at 100°C (ASTM D-445), and a number average molecular weight of between about 1200 to about 4000; more preferred embodiments of this process including at least one of the limitations selected from the following, which may be combined in a manner that would be apparent and practicable to one of ordinary skill in the art in possession of the present disclosure: wherein said feed comprises 10-90 % 1-decene monomer units and 90-10 % 1-dodecene monomer units, on a molar basis; wherein said feed comprises 25-74 % 1-decene monomer units and 75-25 % 1-dodecene monomer units, on a molar basis; wherein said feed comprises 40-60 % 1-decene monomer units and 60-40 % 1-dodecene monomer units, on a molar basis; wherein said feed comprises 45-55 % 1-decene monomer units and 55-45 % 1-dodecene monomer units, on a molar basis; wherein said PAO has a kinematic viscosity of about 40 cSt at 100°C (ASTM D-445), a viscosity index of at least about 150 (ASTM D-2270), and a pour point of less than or equal to about -42°C (ASTM D-97); wherein said PAO has a kinematic viscosity of about 100 cSt at 100°C (ASTM D-445), a viscosity index of at least about 170 (ASTM D-2270), and a pour point of less than or equal to about -30°C (ASTM D-97); wherein said feed further comprises a diluent; wherein said diluent comprises at least one hydrocarbon fluid selected from C6-C13 paraffinic fluids; wherein said oligomerization catalyst is selected from AlCl3, AlBr3, and mixtures thereof; wherein said oligomerization catalyst is an AlCls-water complex having 0.5 moles of water per mole of AlCl3; wherein said oligomerization reaction zone comprises a continuous stirred tank reactor (CSTR); wherein said oligomerization reaction zone comprises more than one oligomerization reactor in series; wherein the oligomerization conditions in said reactor include a temperature of from about 26 and 60°C and a pressure of from about atmospheric to about 50 psia; further comprising a step of distillation to remove unreacted monomeric and dimeric species, followed by hydrogenation of the resulting product, without further separation, to saturate the oligomers, followed by recovery of said PAO; and also a preferred embodiment including a composition made by any one or more of the preceding processes, as would be apparent and practicable to one of ordinary skill in the art in possession of the present disclosure, and/or also additional limitations that are more preferred which are selected from at least one of the following: wherein said at least one PAO comprising C30-C36 trimers, C40-G48 tetramers, and C50-C60 tetramers of 1-decene and 1-dodecene; and wherein said at least one PAO is selected from a PAO having a viscosity of about 40 cSt at 100°C, a PAO having a viscosity of about 100 cSt at 100°C.
[0065] Trade names used herein are indicated by a ™ symbol or ® symbol, indicating that the names may be protected by certain trademark rights, e.g., they may be registered trademarks in various jurisdictions. All patents and patent applications, test procedures (such as ASTM methods, UL methods, and the like), and other documents cited herein are fully incorporated by reference to the extent such disclosure is not inconsistent with this invention and for all jurisdictions in which such incorporation is permitted. When numerical lower limits and numerical upper limits are listed herein, ranges from any lower limit to any upper limit are contemplated.









We Claim:
1. A process for producing a polyalphaolefin (PAO) comprising contacting a feed comprising an olefin mixture, the olefin mixture consisting of 40 to 60% 1-decene monomer units and 60 to 40% 1-dodecene monomer units, on a molar basis, with an oligomerization catalyst, the oligomerization catalyst being an aluminum halide complexed with water, and optionally a diluent, in an oligomerization reaction zone under oligomerization conditions for a time sufficient to produce a PAO having a viscosity of from about 40 cSt to about 100 cSt at 100°C (ASTM D445), and a number average molecular weight of from about 1200 to about 40001 and optionally distilling and hydrogenating the PAO.
2. The process as claimed in claim 1, wherein said feed comprises 45-55% 1-decene monomer units and 55-45% 1-dodecene monomer units, on a molar basis.
3. The process as claimed in claim 1, wherein said PAO has a kinematic viscosity of about 40 cSt at 100°C (ASTM D-445), a viscosity index of at least about 150 (ASTM D-2270), and a pour point of less than or equal to about -42°C (ASTM D-97).
4. The process as claimed in claim 1, wherein said PAO has a kinematic viscosity of about 100 cSt at 100°C (ASTM D-445), a viscosity index of at least about 170 (ASTM D-2270), and a pour point of less than or equal to about -30°C (ASTM D-97).
5. The process as claimed in claim 1, wherein said feed comprises a diluent.
6. The process as claimed in claim 5, wherein said diluent comprises at least one hydrocarbon fluid selected from C6-C13 paraffinic fluids.
7. The process as claimed in claim 1, wherein said oligomerization catalyst is selected from AICl3, AlBr3 and mixtures thereof.
8. The process as claimed in claim 1, wherein said oligomerization catalyst is an AlCl3-water complex having 0.5 moles of water per mole of AlCl3.
9. The process as claimed in claim 1, wherein said oligomerization reaction zone comprises a continuous stirred tank reactor (CSTR).
10. The process as claimed in claim 1, wherein said oligomerization reaction zone comprises more than one oligomerization reactor in series.
11. The process as claimed in claim 1, wherein said oligomerization conditions include a temperature of from about 26 and 60°C and a pressure of from about atmospheric to about 50 psia.
12. The process as claimed in claim 1, wherein the PAO is distilled to remove unreacted monomelic and dimeric species, followed by hydrogenation of the resulting product, without further separation, to saturate the oligomers, followed by recovery of said PAO.
13. The PAO produced by the process as claimed in claim 1.
14. The PAO as claimed in claim 13, said PAO comprising C30-C36 trimers, C40-C48 tetramers, and C50-C60 tetramers of 1-decene and 1-dodecene.
15. The PAO as claimed in claim 13, wherein said PAO is selected from a PAO having a viscosity of about 40 cSt at 100°C, a PAO having a viscosity of about 100 cSt at 100°C, and mixtures thereof.

Documents:

4621-DELNP-2006-Abstract-(21-01-2011).pdf

4621-DELNP-2006-Claims-(21-01-2011).pdf

4621-DELNP-2007-Abstract-(21-01-2011).pdf

4621-delnp-2007-abstract.pdf

4621-DELNP-2007-Assignment-(04-07-2007).pdf

4621-DELNP-2007-Claims-(21-01-2011).pdf

4621-delnp-2007-claims.pdf

4621-DELNP-2007-Correspondence-Others-(02-12-2010).pdf

4621-DELNP-2007-Correspondence-Others-(21-01-2011).pdf

4621-DELNP-2007-Correspondence-Others-(28-01-2011).pdf

4621-delnp-2007-correspondence-others-1.pdf

4621-delnp-2007-correspondence-others.pdf

4621-delnp-2007-description (complete).pdf

4621-DELNP-2007-Form-1-(21-01-2011).pdf

4621-delnp-2007-form-1.pdf

4621-delnp-2007-form-18.pdf

4621-DELNP-2007-Form-2-(21-01-2011).pdf

4621-delnp-2007-form-2.pdf

4621-DELNP-2007-Form-3-(28-01-2011).pdf

4621-delnp-2007-form-3.pdf

4621-delnp-2007-form-5.pdf

4621-DELNP-2007-GPA-(02-12-2010).pdf

4621-DELNP-2007-GPA-(21-01-2011).pdf

4621-delnp-2007-pct-101.pdf

4621-delnp-2007-pct-106.pdf

4621-delnp-2007-pct-210.pdf

4621-delnp-2007-pct-220.pdf

4621-delnp-2007-pct-237.pdf

4621-DELNP-2007-Petition 137-(28-01-2011).pdf


Patent Number 248477
Indian Patent Application Number 4621/DELNP/2007
PG Journal Number 29/2011
Publication Date 22-Jul-2011
Grant Date 18-Jul-2011
Date of Filing 15-Jun-2007
Name of Patentee EXXONMOBIL CHEMICAL PATENTS INC,
Applicant Address 5200 BAYWAY DRIVE, BAYTOWN, TEXAS 77520-2101, USA.
Inventors:
# Inventor's Name Inventor's Address
1 PHIL SURANA 122 SUNNYVALE COURT, SOMERSET, NEW JERSEY 08873, USA.
2 NORMAN YANG 2 NORMANDY DRIVE, WESTFIELD, NEW JERSEY 01090, USA
3 PRAMOD J.NANDAPURKAR 1 MARION DRIVE, PLAINSBORO, NEW JERSEY 08536, USA
PCT International Classification Number C07C 2/22
PCT International Application Number PCT/US2005/045993
PCT International Filing date 2005-12-16
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 11/036,904 2005-01-14 U.S.A.