Title of Invention

A METHOD FOR HYDROPROCESSING A HYDROCARBON FEEDSTOCK

Abstract This invention is directed to a process for hydroprocessing vacuum gas oils and other feeds in order to produce unconverted oil suitable for use as base oil feed for white oils, Group III oils, and BMCI (Bureau of Mines Correlation Index) ethylene plant feed. Ammonia, hydrogen sulfide, and light products are removed from the first stage at high pressure in order to produce a higher quality of unconverted oil that is suitable for Group III base oils.
Full Text

The present invention relates to a method for hydroprocessing a
hydrocarbon feedstock. In addition to gases and middle distillates,
this process can produce unconverted oil which is suitable for use as base oil feed for white oils, Group III oils, and low BMCI (Bureau of Mines Correlation Index) ethylene plant feed.
BACKGROUND OF THE INVENTION
Suitable base stocks for Group III oils.have traditionally been produced in a variety of ways. U.S. Pat. No. 6,136,181 (Ziemer) discloses a process for hydrofinishing and hydrocracking feeds containing sulfur and nitrogen to produce base stocks suitable for use in preparation of Group III oils and white oils. A catalyst comprising a platinum-palladium alloy is employed.
U.S. Pat. No. 6,099,719 (Cody et al.) discloses a process for the preparation of lube oil basestocks suitable for Group III oils. A lube oil feedstock is subjected to solvent extraction and solvent dewaxing prior to a two-step hydroconversion process, which is followed by hydrofinishing and dewaxing steps.
U.S. Pat. No. 5,580,442 (Kwon et al.) employs recycle of unconverted oil to produce high quality lube base oil. VGO is produced by vacuum distillation, then hydrotreated. The hydrotreated VGO is then hydrocracked and light hydrocarbons, along with light oil products, are removed. A portion of the unconverted oil is fed to a second vacuum distillation unit. Material not converted to products in the vacuum distillation unit is recycled to the hydrocracker.

1 Another approach to obtaining Group III basestocks involves two-stage
2 hydroprocessing, in which the effluent from a first stage operated at low
3 pressure is mixed with second stage effluent. The resultant mixture is sent to
4 the fractionation section for product recovery at low pressure. Often a bleed
5 stream from the unconverted oil is taken for feed to the downstream units
6 (such as Group III base oil production or ethylene cracking). The quality of
7 this unconverted oil is not sufficiently high, without further processing to be
8 used as Group III base oil feed or low Bureau of Mines Correlation Index
9 ethylene plant feed. 10
11 SUMMARY OF THE INVENTION
12
13 In the configuration of this invention, the feed to the second stage is a mixture
14 of first and second stage unconverted oil. The first stage is operated at high
15 pressure and the second stage is operated at a lower pressure. The feed to
16 the second stage is high quality unconverted oil, and may be used as feed for
17 Group III base oil production, ethylene plant feed, white oil production, etc. 18
19 The invention is summarized below:
20
21 1. A method for hydroprocessing a hydrocarbon feedstock which produces
22 a stream of unconverted oil of sufficient quality for use as a base oil feed
23 for the production of Group III oils, white oils, and low BMCI ethylene
24 plant feed, said method employing multiple reaction zones within a
25 single reaction loop, comprising the following steps: 26
27 (a) passing a hydrocarbonaceous feedstock to a first hydroprocessing
28 zone, the hydroprocessing zone having one or more beds
29 containing hydroprocessing catalyst, the hydroprocessing zone
30 being maintained at hydroprocessing conditions, including a
31 pressure in the range from 1200 to 2500 psig, wherein the
32 feedstock is contacted with catalyst and hydrogen;

33 (b) passing the effluent of step (a) directly to a hot high pressure
34 ' stripper, wherein the effluent is contacted with a hydrogen-rich

3 stripping gas to produce a vapor stream comprising hydrogen,
4 hydrocarbonaceous compounds boiling at a temperature below the
5 boiling range of the hydrocarbonaceous feedstock, hydrogen
6 sulfide, ammonia, and a bottoms stream comprising
7 hydrocarbonaceous compounds boiling in approximately the same
8 range of said hydrocarbonaceous feedstock along with a portion of
9 the hydrocarbonaceous compounds boiling in the diesel boiling
10 range;
11 (c) passing the overhead vapor stream from the hydrogen stripper of
12 step (b) to a first cold high pressure separator where hydrogen,
13 hydrogen sulfide and light hydrocarbonaceous gases are removed
14 overhead and a liquid stream comprising naphtha, middle distillates
15 and unconverted oil is passed to fractionation, thereby removing
16 most of the ammonia and some of the hydrogen sulfide (as
17 ammonium bi-sulfide in the sour water stream as it leaves the cold
18 high-pressure separator);
19 (d) combining the liquid stream from the hydrogen stripper of step (b)
20 with a portion of the unconverted oil of the fractionation step of
21 step (c) and passing the combined stream to a bed of
22 hydroprocessing catalyst in a second reactor zone, wherein the
23 liquid is contacted under hydroprocessing conditions with the
24 catalyst, in the presence of hydrogen, and under a pressure in the
25 range from 1500 to 2500 psig;
26 (e) passing the overhead from the cold high pressure separator of
27 step (d) to an amine absorber, where hydrogen sulfide is removed
28 before hydrogen is compressed and recycled to hydroprocessing
29 vessels within the loop;

1 (f) passing the effluent of step (d), after cooling, to a second cold high
2 pressure separator where hydrogen, hydrogen sulfide and light
3 hydrocarbonaceous gases are removed overhead and a liquid
4 stream comprising naphtha, middle distillates and unconverted oil
5 is passed to fractionation, thereby removing most of the ammonia
6 and some of the hydrogen sulfide (as ammonium bi-sulfide in the
7 sour water stream as it leaves the second cold high-pressure
8 separator);
9 (g) passing the vapor stream from step (f) after further cooling and
10 separation of condensate, to the recycle gas hydrogen
11 compressor;
12 (h) passing the compressed hydrogen from the recycle gas
13 compressor to the primary reactor loop; and
14 (i) passing at least a portion of the unconverted oil from the
15 fractionator of steps (c) and (f) to facilities for the preparation of
16 Group III oil, white oil, or BMCI ethylene feed. 17

18 The instant invention provides reduced capital investment and operating
19 costs, as compared with the traditional two stage hydroprocessing scheme. 20
21 BRIEF DESCRIPTION OF THE FIGURE
22
23 The Figure illustrates a two-stage hydroprocessing unit adapted for use in the
24 instant invention. Hydrotreating preferably occurs in the first stage, while
25 hydrocracking preferably occurs in the second stage. 26

1 DETAILED DESCRIPTION OF THE INVENTION
2
3 Description of the Preferred Embodiment
4
5 A hydrocarbon feed (stream 1) preferably comprising gas oil in combination
6 with nitrogen (although other hydrocarbon feeds containing nitrogen may be
7 employed) is combined with hydrogen (stream 2) and heated in heat
8 exchanger 3. The feed is then passed, through stream 6, to exchanger 4.
9 Stream 7 exits the heat exchanger and passes to furnace 8 for further 10 heating.
11
12 Stream 9 exits the furnace and enters the first-stage hydroprocessor, in which
13 the stream is contacted with hydrotreating catalyst in one or more beds.
14 Hydrogen may be employed as an interbed quench, as illustrated by streams
15 11 and 12. In the first-stage hydroprocessor, the oil feed is hydrotreated and
16 partially converted into products. Stream 13, the hydroprocessor effluent,
17 comprises light vaporized hydrocarbons, distillate oils, heavy unconverted oil,
18 and excess hydrogen not consumed in the reaction.
19
20 Stream 13 is slightly cooled in heat exchanger 4, by heat exchange with
21 stream 6, the feed to the first stage hydroprocessor. The cooled stream, now
22 stream 14, passes to high pressure stripper 15. A part of the make-up
23 hydrogen (stream 2) is used as the stripping media.
24
25 Vapor from the high pressure stripper 15 (stream 26) is first cooled by process
26 streams (not shown) and then by an air cooler (not shown) before passing to
27 the cold high pressure separator 20. Wash water (stream 27) is continually
28 injected upstream of the air cooler to prevent the deposition of salts in the air
29 cooler tubes.
30
31 In the cold high pressure separator 20, the cooled first stage effluent, line 49
32 is separated into its hydrogen-rich vapor (stream 29), hydrocarbon liquid
33 (stream 32), and water phases (stream 28) in the cold high pressure

34 separator 20. The sour water stream 28, which contains ammonium bisulfide,
35 is sent to sour water stripping. The hydrocarbon liquid effluent of the cold
36 high pressure separator 20, line 32, is combined with the hydrocarbon liquid
37 from the cold high pressure separator 30 (stream 37) to create line 38, which
38 enters fractionator 35. The hydrocarbon stream is heated and distilled into
39 product streams illustrated, gas 42, naphtha 43, kerosene 44, diesel 46 and
40 bottoms 47. 8
9 The second stage reactor 10 converts the unconverted oil from the first stage
10 into products. Hydrogen enters as interbed quench through streams 19, 21
11 and 22. The second-stage reactor effluent, stream 23, consists of light
12 vaporized hydrocarbons, distillate oils, heavy unconverted oil, and excess
13 hydrogen not consumed in the reaction. This effluent stream is cooled by
14 heat exchange (exchanger 3) with the process streams (stream 1) and finally
15 with an air cooler (not shown) before it passes, in stream 24, to the cold high
16 pressure separator 30. The hydrogen rich gas (stream 33) flows into
17 knockout drum 40. Stream 41 exits the knockout drum 40 as stream 41 and
18 passes to the recycle gas compressor 39. Recycle compressor 39 delivers
19 the recycle gas to the reactor loop in stream 48. Part of the recycle
20 compressor discharge gas is routed to the first-stage reactor as quench
21 (streams 11 and 12) to control the reactor temperature. The remaining
22 recycle gas that is not used as quench in either the first or second stage
23 (streams 19, 21 and 22 for the second stage) is combined with the make-up
24 hydrogen (stream 2) to become the first-stage reactor feed gas. The
25 first-stage reactor feed gas is heated by process streams before combining
26 with the first-stage oil feed. 27
28 Feeds
29
30 A wide variety of hydrocarbon feeds may be used in the instant invention.
31 Typical feedstocks include any heavy or synthetic oil fraction or process
32 stream having a boiling point above 392°F (200°C). Such feedstocks include
33 vacuum gas oils, heavy atmospheric gas oil, delayed coker gas oil, visbreaker

34 gas oil demetallized oils, vacuum residua, atmospheric residua, deasphalted
35 oil, Fischer-Tropsch streams, and FCC streams. An upgraded base stock
36 useful as a feedstock to the hydrotreater process preferably contains less
37 than about 200 ppm sulfur and about 100 ppm nitrogen, and has a viscosity
38 index of greater than about 80, with a viscosity index of greater than 85 and
39 even greater than 90 being preferred. 7

8 Lubricating oil base stocks that are suitable for use in the present invention
9 also may be recovered from a solvent extraction process. In solvent

10 extraction, a distillate fraction, generally a vacuum gas oil, which optionally
11 has been desulfurized, is contacted with a solvent, such as N-methyl
12 pyrrolidone or furfural, in a solvent extraction zone, preferably employing a
13 countercurrent extraction unit. The aromatics-lean raffinate is stripped of
14 solvent, optionally dewaxed, and subsequently hydrogenated to improve
15 product stability and color. The recovered solvent is usually recycled. 16
17 Products
18
19 Group III base stocks, with greater than or equal to 90% saturates, less than
20 or equal to 0.03 percent sulfur, and with a viscosity index greater than or
21 equal to 120, may be produced from this invention. Test methods for
22 evaluating group category properties including: saturates-ASTM D-2007;
23 viscosity index-ASTM D2270; sulfur-one of ASTM D-2622, ASTM D-4294,
24 ASTM D-4927, ASTM D-3120. The viscosity of the finished lube oil, when
25 measured at 100°C (212°F), is generally greater than 2 cSt. 26

27 A white oil base stock may also be prepared from this invention. A white oil is
28 defined herein as a mineral oil which may be safely used in food/food
29 packaging. It is a mixture of liquid hydrocarbons, essentially paraffinic and
30 naphthenic in nature obtained from petroleum. It is refined to meet the test
31 requirements of the United States Pharmacopeia (U.S.P.)XX (1980), at
32 page 532, for readily carbonizable substances. It also meets the test
33 requirements of U.S.P. XVII for sulfur compounds at page 400.

34 A white oil produced in the present process meets the requirements of
35 regulation 21 CFR 172.878, 21 CFR 178.3620(a), 21 CFR 178.3620(b), or
36 21 CFR 178.3620(c), all refer to Apr. 1, 1996 edition, for USP and technical
37 grade white oils, which regulations of its Apr. 1,1996 edition are incorporated
38 herein by reference. 6

7 Emphasis is placed on the lube base stock feeds that may be produced from
8 this invention, but the process of this invention is also useful in the production
9 of middle distillate fractions boiling in the range of about 250-700°F

10 (121-371°C). A middle distillate fraction is defined as having an approximate
11 boiling range from about 250°F to 700°F. At least 75 vol %, preferably
12 85 vol %, of the components of the middle distillate has a normal boiling point
13 of greater than 250°F. At least about 75 vol %, preferably 85 vol %, of the
14 components of the middle distillate has a normal boiling point of less than
15 700°F. The term "middle distillate" includes the diesel, jet fuel and kerosene
16 boiling range fractions. The kerosene or jet fuel boiling point range refers to
17 the range between 280°F and 525°F (38-274°C). The term "diesel boiling
18 range" refers to hydrocarbons boiling in the range from 250°F to 700°F
19 (121-371°C). 20

21 Gasoline and naphtha may also be produced in this invention. Gasoline or
22 naphtha normally boils in the range below 400°F (204°C), or C10-. Boiling
23 ranges of various product fractions recovered in any particular refinery will
24 vary with such factors as the characteristics of the crude oil source, local
25 refinery markets, and product prices. 26
27 Conditions
28
29 The first stage of the instant invention is directed to hydrotreating of
30 lubricating oil base stocks. The hydrogenation reaction takes place in the
31 presence of hydrogen, preferably at hydrogen pressures in the range of
32 between about 500 psig and 5000 psig, more preferably in the range of about

33 1200 psig to about 2500 psig. The feed rate to the hydrogenation catalyst
34 system is in the range of from about 0.1 to about 5 LHSV, preferably in the
35 range of about 0.2 to about 1.5 LHSV. The hydrogen supply (make-up and
36 recycle) is in the range of from about 500 to about 20,000 standard cubic feet
37 (SCF) per barrel of liquid hydrocarbon feed, preferably in the range of from
38 about 2000 to about 10, 000 standard cubic feet per barrel. 7
8 Hydroprocessing conditions are a general term which refers primarily in this
9 application to hydrocracking or hydrotreating, preferably hydrocracking. The
10 first stage reactor, as depicted in Figure 1, is a hydrotreating zone.
11
12 Typical hydrocracking conditions include a reaction temperature of from
13 400°F-950°F (204°C-510°C), preferably 650°F-850°F (343°C-454°C).
14 Reaction pressure ranges from 500 to 5000 psig (3.5-4.5 MPa), preferably
15 1500-3500 psig, and more preferably in the range from 1500 to 2500 psig.
16 LHSV ranges from 0.1 to 15 hr"1 (v/v), preferably 0.25-2.5 hr"1. Hydrogen
17 consumption ranges from 500 to 2500 SCF per barrel of liquid hydrocarbon
18 feed (89.1-445m3 H2/m3feed). 19
20 Catalyst
21
22 Each hydroprocessing zone may contain only one catalyst, or several
23 catalysts in combination. 24

25 Hydrotreating catalyst usually is designed to remove sulfur and nitrogen and
26 provide a degree of aromatic saturation. It will typically be a composite of a
27 Group VI metal or compound thereof, and a Group VIII metal or compound
28 thereof supported on a porous refractory base such as alumina. Examples of
29 hydrotreating catalysts are alumina supported cobalt-molybdenum, nickel
30 sulfide, nickel-tungsten, cobalt-tungsten and nickel-molybdenum. Typically,
31 such hydrotreating catalysts are presulfided. 32

32 The hydrocracking catalyst generally comprises a cracking component, a
33 hydrogenation component, and a binder. Such catalysts are well known in the
34 art. The cracking component may incluae an amorphous silica/alumina phase
35 and/or a zeolite, such as a Y-type or USY zeolite. Catalysts having high
36 cracking activity often employ REX, REY and USY zeolites. The binder is
37 generally silica or alumina. The hydrogenation component will be a Group VI,
38 Group VII, or Group VIII metal or oxides or sulfides thereof, preferably one or
39 more of iron, chromium, molybdenum, tungsten, cobalt, or nickel, or the
40 sulfides or oxides thereof. If present in the catalyst, these hydrogenation

10 components generally make up from about 5% to about 40% by weight of the
11 catalyst. Alternatively, noble metals, especially platinum and/or palladium,
12 may be present as the hydrogenation component, either alone or in
13 combination with the base metal hydrogenation components iron, chromium
14 molybdenum, tungsten, cobalt, or nickel. If present, the platinum group
15 metals will generally make up from about 0.1% to about 2% by weight of the
16 catalyst. 17
18 Catalyst selection is dictated by process needs and product specifications.



WE CLAIM:
1
2
3 1. A method for hydroprocessing a hydrocarbon feedstock which produces
4 a stream of unconverted oil of sufficient quality for use as a base oil feed
5 for the production of Group 111 oils, white oils and low BMCI ethylene
6 plant feed, said method employing multiple reaction zones within a
7 single reaction loop, comprising the following steps: 8
9 (a) passing a hydrocarbonaceous feedstock to a first hydroprocessing
10 zone, the hydroprocessing zone having one or more beds
11 containing hydroprocessing catalyst, the hydroprocessing zone
12 being maintained at hydroprocessing conditions, including a
13 pressure in the range from 500 to 5000 psig, wherein the feedstock
14 is contacted with catalyst and hydrogen; 15
16 (b) passing the effluent of step (a) directly to a hot high pressure
17 stripper, wherein the effluent is contacted with a hydrogen-rich
18 stripping gas to produce a vapor stream comprising hydrogen,
19 hydrocarbonaceous compounds boiling at a temperature below the
20 boiling range of the hydrocarbonaceous feedstock, hydrogen
21 sulfide, ammonia, and a bottoms stream comprising
22 hydrocarbonaceous compounds boiling in approximately the same
23 range of said hydrocarbonaceous feedstock along with a portion of
24 the hydrocarbonaceous compounds boiling in the diesel boiling
25 range;
26
27 (c) passing the overhead vapor stream from the hydrogen stripper of
28 step (b) to a first cold high pressure separator where hydrogen,
29 hydrogen sulfide and light hydrocarbonaceous gases are removed
30 overhead and a liquid stream comprising naphtha, middle distillates
31 and unconverted oil is passed to fractionation, thereby removing
32 most of the ammonia and some of the hydrogen sulfide (as

33 ammonium bi-sulfide in the sour water stream as it leaves the cold
34 high-pressure separator); 3
4 (d) combining the liquid stream from the hydrogen stripper of step (b)
5 with a portion of the unconverted oil of the fractionation step of
6 step (c) and passing the combined stream to a bed of
7 hydroprocessing catalyst in a second reactor zone, wherein the
8 liquid is contacted under hydroprocessing conditions with the
9 catalyst, in the presence of hydrogen, and under a pressure in the 10 range from 500 to 5000 psig;
11
12 (e) passing the overhead from the cold high pressure separator of
13 step (d) to an amine absorber, where hydrogen sulfide is removed
14 before hydrogen is compressed and recycled to hydroprocessing
15 vessels within the loop; 16
17 18 pressure separator where hydrogen, hydrogen sulfide and light
19 hydrocarbonaceous gases are removed overhead and a liquid
20 stream comprising naphtha, middle distillates and unconverted oil
21 is passed to fractionation, thereby removing most of the ammonia
22 and some of the hydrogen sulfide (as ammonium bi-sulfide in the
23 sour water stream as it leaves the second cold high-pressure
24 separator); 25
26 (g) passing the vapor stream from step (f) after further cooling and
27 separation of condensate, to the recycle gas hydrogen
28 compressor;
29
30 (h) passing the compressed hydrogen from the recycle gas hydrogen
31 compressor to the primary reactor loop; and
32

(i) passing at least a portion of the unconverted oil from the fractionator of steps (c) and (f) to facilities for the preparation of Group III oil, white oil, or BMCI ethylene feed.
2. The process as claimed in claim 1, in which hydrotreating occurs in the first hydroprocessing zone and hydrocracking occurs in the second hydroprocessing zone.
3. The process as claimed in claim 1, wherein the hydroprocessing conditions of claim 1, step (a), comprise a reaction temperature of from 400°F-950°F (204°C-510°C), a reaction pressure in the range from 1200 to 2500 psig, an LHSV in the range from 0.1 to 15 hr'1 (v/v), and hydrogen consumption in the range from 500 to 2500 scf per barrel of liquid hydrocarbon feed (89.1-445 m3 H2/m3 feed.
4. The process as claimed in claim 3, wherein the hydroprocessing conditions of claim 1, step (a), preferably comprise a temperature in the range from 650°F-850°F (343°C-454°C)? reaction pressure in the range from 1200 to 2500 psig an LHSV in the range from 0.25 to 2.5 hr"1, and hydrogen consumption in the range from 500 to 2500 scf per barrel of liquid hydrocarbon feed (89.1-445 m3H2/m3 feed.
5. The process as claimed in claim 1, wherein the hydroprocessing conditions of claim 1, step (d), comprise a reaction temperature of from 400°F-950°F (204°C-510°C), a reaction pressure in the range from 500 to 5000 psig), an LHSV in the range from 0.1 to 15 hr'1 (v/v), and hydrogen consumption in the range from 500 to 2500 scf per barrel of liquid hydrocarbon feed (89.1-445 m3 H2/m3 feed).

6. The process as claimed in claim 5, wherein the hydroprocessing conditions of claim 1, step (d), preferably comprise a temperature in the range from 650°F-850°F (343°C-454°C), reaction pressure in the range from 1500 to 2500 psig, LHSV in the range from 0.25 to 2.5 h'1, and hydrogen consumption in the range from 500 to 2500 scf per barrel of liquid hydrocarbon feed (89.1-445 m3 H2/m3 feed).
7. The process as claimed in claim 1, wherein the feed to claim 1, step (a), comprises hydrocarbons boiling above 392°F (200°C).
8. The process as claimed in claim 7, wherein the feed is selected from the group consisting of vacuum gas oil, heavy atmospheric gas oil, delayed coker gas oil, visbreaker gas oil, demetallized oils, FCC light cycle oil, vacuum residua deasphalted oil, Fischer-Tropsch streams, and FCC streams.
9. The process as claimed in claim 1, wherein the second hydroprocessing zone of step
(d) is maintained at a lower pressure than that of the first hydroprocessing zone of step
(a).
10. The process as claimed in claim 1, in which each hydroprocessing zone may
contain only one catalyst, or several catalysts in combination.


Documents:

1024-chenp-2005 abstract-duplicate.pdf

1024-chenp-2005 abstract.pdf

1024-chenp-2005 claims-duplicate.pdf

1024-chenp-2005 claims.pdf

1024-chenp-2005 correspondence-others.pdf

1024-chenp-2005 description (complete)-duplicate.pdf

1024-chenp-2005 description (complete).pdf

1024-chenp-2005 drawings-duplicate.pdf

1024-chenp-2005 drawings.pdf

1024-chenp-2005 form-1.pdf

1024-chenp-2005 form-18.pdf

1024-chenp-2005 form-26.pdf

1024-chenp-2005 form-3.pdf

1024-chenp-2005 form-5.pdf

1024-chenp-2005 others document.pdf

1024-chenp-2005 others.pdf

1024-chenp-2005 pct.tif

1024-chenp-2005-abstract.pdf

1024-chenp-2005-claims.pdf

1024-chenp-2005-correspondnece-others.pdf

1024-chenp-2005-correspondnece-po.pdf

1024-chenp-2005-description(complete).pdf

1024-chenp-2005-drawings.pdf

1024-chenp-2005-form 1.pdf

1024-chenp-2005-form 18.pdf

1024-chenp-2005-form 26.pdf

1024-chenp-2005-form 3.pdf

1024-chenp-2005-form 5.pdf

1024-chenp-2005-pct.pdf


Patent Number 215399
Indian Patent Application Number 1024/CHENP/2005
PG Journal Number 13/2008
Publication Date 31-Mar-2008
Grant Date 26-Feb-2008
Date of Filing 25-May-2005
Name of Patentee CHEVRON U.S.A. INC
Applicant Address 6001 Bollinger Canyon Road, San Ramon, California 94583,
Inventors:
# Inventor's Name Inventor's Address
1 FARSHID, Darush 19 Hillcrest Avenue, Larkspur, CA 94939,
PCT International Classification Number C10G 69/02
PCT International Application Number PCT/US2003/031869
PCT International Filing date 2003-10-08
PCT Conventions:
# PCT Application Number Date of Convention Priority Country
1 10/282,767 2002-10-28 U.S.A.