DETAILED ACTION
The present application, filed on or after March 16, 2013, is being examined under the first inventor to file provisions of the AIA .
This communication is in response to the election filed 4/10/2026.
Claims 1-8 are pending. Claims 9-13 are canceled.
Election/Restrictions
Applicant’s election without traverse of Group I, claims 1-8 in the reply filed on 4/10/2026 is acknowledged. Claims 9-13 have been canceled.
Double Patenting
The nonstatutory double patenting rejection is based on a judicially created doctrine grounded in public policy (a policy reflected in the statute) so as to prevent the unjustified or improper timewise extension of the “right to exclude” granted by a patent and to prevent possible harassment by multiple assignees. A nonstatutory double patenting rejection is appropriate where the conflicting claims are not identical, but at least one examined application claim is not patentably distinct from the reference claim(s) because the examined application claim is either anticipated by, or would have been obvious over, the reference claim(s). See, e.g., In re Berg, 140 F.3d 1428, 46 USPQ2d 1226 (Fed. Cir. 1998); In re Goodman, 11 F.3d 1046, 29 USPQ2d 2010 (Fed. Cir. 1993); In re Longi, 759 F.2d 887, 225 USPQ 645 (Fed. Cir. 1985); In re Van Ornum, 686 F.2d 937, 214 USPQ 761 (CCPA 1982); In re Vogel, 422 F.2d 438, 164 USPQ 619 (CCPA 1970); In re Thorington, 418 F.2d 528, 163 USPQ 644 (CCPA 1969).
A timely filed terminal disclaimer in compliance with 37 CFR 1.321(c) or 1.321(d) may be used to overcome an actual or provisional rejection based on nonstatutory double patenting provided the reference application or patent either is shown to be commonly owned with the examined application, or claims an invention made as a result of activities undertaken within the scope of a joint research agreement. See MPEP § 717.02 for applications subject to examination under the first inventor to file provisions of the AIA as explained in MPEP § 2159. See MPEP § 2146 et seq. for applications not subject to examination under the first inventor to file provisions of the AIA . A terminal disclaimer must be signed in compliance with 37 CFR 1.321(b).
The filing of a terminal disclaimer by itself is not a complete reply to a nonstatutory double patenting (NSDP) rejection. A complete reply requires that the terminal disclaimer be accompanied by a reply requesting reconsideration of the prior Office action. Even where the NSDP rejection is provisional the reply must be complete. See MPEP § 804, subsection I.B.1. For a reply to a non-final Office action, see 37 CFR 1.111(a). For a reply to final Office action, see 37 CFR 1.113(c). A request for reconsideration while not provided for in 37 CFR 1.113(c) may be filed after final for consideration. See MPEP §§ 706.07(e) and 714.13.
The USPTO Internet website contains terminal disclaimer forms which may be used. Please visit www.uspto.gov/patent/patents-forms. The actual filing date of the application in which the form is filed determines what form (e.g., PTO/SB/25, PTO/SB/26, PTO/AIA /25, or PTO/AIA /26) should be used. A web-based eTerminal Disclaimer may be filled out completely online using web-screens. An eTerminal Disclaimer that meets all requirements is auto-processed and approved immediately upon submission. For more information about eTerminal Disclaimers, refer to www.uspto.gov/patents/apply/applying-online/eterminal-disclaimer.
Claims 1-8 rejected on the ground of nonstatutory double patenting as being unpatentable over claims 12-19 of U.S. Patent No. 10,954,456.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patent fails to claim the boiling point of the by-product hydrocarbon in the product mixture. However, given the same feed is reacted to produce the same Product Heavy Marine Fuel Oil compliant with ISO 8217:2017 Table 2, it would have been obvious to one of ordinary skill in the art at the time that the biproduct would boil in a range overlapping that claimed.
Claims 1-8 rejected on the ground of nonstatutory double patenting as being unpatentable over claims 1-23 of U.S. Patent No. 11,441,084.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patent fails to claim the boiling point of the by-product hydrocarbon in the product mixture. However, given the same feed is reacted to produce the same Product Heavy Marine Fuel Oil compliant with ISO 8217:2017 Table 2, it would have been obvious to one of ordinary skill in the art at the time that the biproduct would boil in a range overlapping that claimed.
Claims 1-8 rejected on the ground of nonstatutory double patenting as being unpatentable over claims 1-10 of U.S. Patent No. 11,884,883.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patent fails to claim the boiling point of the by-product hydrocarbon in the product mixture. However, given the same feed is reacted to produce the same Product Heavy Marine Fuel Oil compliant with ISO 8217:2017 Table 2, it would have been obvious to one of ordinary skill in the art at the time that the biproduct would boil in a range overlapping that claimed.
Claims 1-8 are rejected on the ground of nonstatutory double patenting as being unpatentable over claims 1-16 of U.S. Patent No. 12,139,672.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patents claims fail to teach the boiling point of the by-product in the product mixture, specifically wherein said Process Mixture comprises a Product Heavy Marine Fuel Oil, by-product hydrocarbons having a boiling point less than 150 F, and bulk gases. However, given the same feed, process, and products are produced, and the same Product Heavy Marine Fuel Oil, ISO 8217:0217 table 2 residual marine fuel, is produced, it would have been obvious to one of ordinary skill in the art at the time of filing to separate all products boiling less than 150F to isolate the desired product fraction.
HMFO = HMFO
US 10954456 B2
Claims 12-19
US 11441084 B2
Claims 1-23
US 11884883 B2
Claims 1-10
US 12139672 B2
Claims 1-16
1. A process for the production of a Product HMFO, the process comprising:
12. A process for the production of a HMFO, the process comprising:
1. A process for the production of a Product HMFO, the process comprising:
1. A process for the production of a Product HMFO, the process comprising:
1,9. A process for the production of a Product HMFO, the process comprising:
mixing a quantity of a HMFO feed with a quantity of an Activating Gas to give a Feedstock Mixture,
mixing a quantity of said Feedstock HMFO, with a quantity of Activating Gas mixture to give a Feedstock Mixture;
mixing a quantity of a HMFO feed with a quantity of an Activating Gas to give a Feedstock Mixture,
mixing a quantity of a HMFO feedstock with a quantity of an Activating Gas to give a Feedstock Mixture,
a. mixing a quantity of a HMFO with a quantity of an Activating Gas to give a Feedstock Mixture,
wherein said HMFO feed complies with ISO 8217 (2017) Table 2 as a residual marine fuel, except one or more Environmental Contaminants selected from the group consisting of: sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, at a combined concentration > 0.5% wt.;
wherein said Feedstock HMFO complies with ISO 8217(2017) and said Feedstock HMFO has a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 mass % to 1.0 mass %,
wherein said HMFO feed complies with ISO 8217 (2017) as a residual marine fuel, except one or more Environmental Contaminants selected from the group consisting of: sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, at a combined concentration > 0.5% wt.;
immediately prior to mixing said HMFO feedstock is compliant with ISO 8217 (2017) as a Table 2 residual marine fuel, except 1+ Environmental Contaminants selected from the group consisting of: sulfur; vanadium, nickel, iron, aluminum and silicon & combinations thereof, with a combined concentration > 0.5% wt.
immediately prior to mixing said HMFO is compliant with ISO 8217 (2017) as a Table 2 residual marine fuel, except one or more Environmental Contaminants selected from the group consisting of: sulfur; vanadium, nickel, iron, aluminum and silicon & combinations thereof with a combined concentration > 0.5% wt.;
contacting the Feedstock Mixture with one or more catalysts under hydrotreating reactive conditions in a Reaction System to form a Process Mixture from said Feedstock Mixture,
contacting said Feedstock Mixture with 1+ catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture; 15 Reaction conditions16,17,19 Specific hydrotreating catalysts
contacting said Feedstock Mixture with 1+ catalyst under reactive conditions . . . forming a Process Mixture,
9,12 Reaction Conditions
distributing said Feedstock Mixture to a Reaction System, wherein the Reaction System is comprised of one or more reactor vessels, and
6,10 Reaction conditions
b. providing said Feedstock Mixture to a Reaction System, reactive conditions for catalytic hydrogenation of the Feedstock8,16 Reaction Conditions
wherein each of said reactor train is configured with at least two reactor vessels in series, and
At least three reactor vessels are arranged in series form a first reactor train and at least three reactor vessels in series form a second reactor train,
2. the Reaction System is comprised of five or more reactor vessels, two parallel trains of two reactors each in series with a third downstream reactor
2. the Reaction System is comprised of six reactor vessels in two parallel trains of three sequential reactors each
4. the reaction system includes two trains in parallel of three reactors each in series
wherein each reactor vessel is independently selected from the group consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebullated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor, fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations thereof,
wherein said reactor vessels ae selected from the group consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebulliated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor, fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations thereof,
each is independently selected from the group of operational configurations consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebulliated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor, fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations thereof,
each is independently selected from the group of operational configurations consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebulliated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor, fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations thereof, and
claim 9. one or more fixed catalyst beds . . . wherein the fixed catalyst bed is dense-loaded or sock loaded with catalyst materials
·each Reaction System is configured such that the Feedstock Mixture is first passed through at least one first reactor vessel containing 1+ catalyst materials selected from the group consisting of hydrodemetallization catalyst, hydro-transition catalyst, inert catalyst materials and combinations thereof; ·then subsequently passed through 1+ second reactor vessel with one or more catalyst selected from the group consisting of hydro-transition catalyst, hydrodesulfurization catalyst, inert catalyst materials, and combinations;
19. the first reactor in each train is loaded with a first catalyst system selected from the group consisting of: a hydrodemetallization catalyst material; a hydrotransition catalyst material; an inert catalyst material; and, combinations thereof, and ·second reactor in each train is loaded with a second catalyst system, wherein the second catalyst system is selected from the group consisting of: a hydrotransition catalyst material, a hydrodesulfurization catalyst material; . . .
· said Reaction System is configured such that the Feedstock Mixture is first distributed and passed through at least one first reactor vessel containing one or more catalyst materials with hydrodemetallization activity; and ·then subsequently distributed and passed through at least one second reactor vessel containing one or more catalyst materials with mixed hydrodemetallization and hydrodesulfurization activity, and
· the Feedstock Mixture is first passed through first bed(s) that contain one or more catalyst materials with hydrodemetallization activity; and · then subsequently passed through second bed(s) that contain one or more catalyst materials with mixed hydrodemetallization and hydrodesulfurization activity, and · subsequently passed through third bed(s) with catalyst having hydrodesulfurization activity,
5. the first and second reactor vessels are loaded with a first catalyst system independently selected from the group consisting of: a hydrodemetallization; a hydrotransition; an inert catalyst material; and, combinations thereof,
· the third reactor is loaded with catalyst selected from the group consisting of: a hydrotransition catalyst material, a hydrodesulfurization catalyst material; an inert catalyst material; and, combinations thereof.
wherein said Process Mixture comprises a Product HMFO, by-product hydrocarbons having a boiling point less than 150 F and bulk gases;
Process mixture comprises bulk gases, by product hydrocarbon and Product HMFO
wherein said Process Mixture comprises one or more bulk gaseous components, one or more liquid hydrocarbon components, and one or more residual gaseous components entrained in said hydrocarbon liquid components, wherein said one or more liquid hydrocarbon components comprises one or more by-product hydrocarbon components and a Product HMFO component;
thereby forming a Process Mixture from said Feedstock Mixture, wherein said Process Mixture comprises one or more bulk gaseous components, one or more liquid hydrocarbon components, and one or more residual gaseous components entrained in said hydrocarbon liquid components, wherein said one or more liquid hydrocarbon components comprises a Product HMFO component;
c. forming a Process Mixture from said Feedstock Mixture, i. wherein said Process Mixture comprises a Product HMFO component;
4 bulk gases
receiving by fluid communication said Process Mixture in at least one separation vessel and separating the Product HMFO from the by-product hydrocarbons and the bulk gases and, discharging said Product HMFO from the at least one separation vessel,
receiving said Process Mixture and separating any liquid components of said Process Mixture from any bulk gaseous components of said Process Mixture; subsequently separating any residual gaseous components and any by-product hydrocarbon components from said Process Mixture to form a Product HMFO; and, discharging said Product HMFO;
receiving . . . in at least one separation vessel and separating the one or more bulk gaseous components of said Process Mixture from a combined one or more liquid hydrocarbon components, and one or more residual gaseous components entrained in said hydrocarbon liquid components; . . . additionally separating the hydrocarbon liquid components into one or more by-product hydrocarbon components and the Product HMFO component; and,
receiving . . . in at least one separation vessel and separating the 1+ bulk gaseous components of said Process Mixture from a combined 1+ liquid hydrocarbon components, and 1+ residual gaseous components entrained in said hydrocarbon liquid components; . . . and separating the Product HMFO component from the combined 1+ liquid hydrocarbon components, and 1+ residual gaseous components entrained in said hydrocarbon liquid components;
d. receiving by fluid communication said Process Mixture in at least one separation vessel; e. separating the Product HMFO component from said Process Mixture in said at least one separation vessel; and,
4. separating 1+ bulk gases from 1+ liquid hydrocarbon components
wherein said Product HMFO complies with ISO 8217:2017 Table 2 as a residual marine fuel and sulfur less than 0.5 wt%
13. Product HMFO complies with ISO 8217 (2017) and said Product HMFO has a sulfur content (ISO 14596 or ISO 8754) between the range of 0.50 mass % to 0.05 mass %.
6, 7, 13 complies with ISO 8217 (2017) as a residual marine fuel + contaminants or sulfur 0.50 mass % to 0.05 mass %.
4,5,8,9 said Product Heavy Marine Fuel Oil complies with ISO 8217 (2017), as a Table 2 residual marine fuel + sulfur 0.50 mass % to 0.05 mass %.
f. discharging said Product HMFO
6,7,14,15 said Product Heavy Marine Fuel Oil discharged by the process complies with ISO 8217 (2017) as a Table 2 residual marine fuel + contaminant or sulfur 0.50 mass % to 0.05 mass %.
Claims 1-8 rejected on the ground of nonstatutory double patenting as being unpatentable over claims 1-19 of U.S. Patent No. 11,492,559.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patent fails to claim the boiling point of the by-product hydrocarbon in the product mixture. However, given the same feed is reacted to produce the same Product Heavy Marine Fuel Oil compliant with ISO 8217:2017 Table 2, it would have been obvious to one of ordinary skill in the art at the time that the biproduct would boil in a range overlapping that claimed.
Claims 1-8 rejected on the ground of nonstatutory double patenting as being unpatentable over claims 1-18 of U.S. Patent No. 11,560,520.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patent fails to claim the boiling point of the by-product hydrocarbon in the product mixture. However, given the same feed is reacted to produce the same Product Heavy Marine Fuel Oil compliant with ISO 8217:2017 Table 2, it would have been obvious to one of ordinary skill in the art at the time that the biproduct would boil in a range overlapping that claimed. Lastly, the patent fails to disclose wherein the two or more reaction vessels are selected from the apparatus claimed. However, the claims are drawn to a process and further hydrotreating reaction vessels are common and would have been obvious given the general knowledge of one in the art.
Claims 1-8 rejected on the ground of nonstatutory double patenting as being unpatentable over claims 1-9 of U.S. Patent No. 10,604,709.
With respect to each of the identified patents, although the claims at issue are not identical, they are not patentably distinct from each other because they claim overlapping process steps and merely fails to claim using series of reactors of a specific type. The patent claim does not explicitly state under hydrotreating reaction conditions but claims the same reaction conditions and catalyst. The patent fails to claim the boiling point of the by-product hydrocarbon in the product mixture. However, given the same feed is reacted to produce the same Product Heavy Marine Fuel Oil compliant with ISO 8217:2017 Table 2, it would have been obvious to one of ordinary skill in the art at the time that the biproduct would boil in a range overlapping that claimed. Lastly, the patent fails to claim wherein the reactor is two or more in series and the vessels are selected from the apparatus claimed. The art claims using multiple catalysts. It is well known to utilizes one or more catalyst across one or more beds and may be positioned in one vessel or separate vessels in hydrotreating along with the specific reaction vessels claimed and therefore such selection would have been obvious.
US 11492559 B2Claims 1-19
US 11560520 B2
Claims 1-18
US 10604709 B2
Claims 1-9
1. A process for the production of a Product HMFO, the process comprising:
1. A process for reducing Environmental Contaminants in a Feedstock HMFO, the process comprising:
1. A process for reducing the Environmental Contaminants and Detrimental Solids in a Feedstock HMFO, the process comprising
1. A process for production of a Product HMFO from Distressed Fuel Oil Materials, the process comprising:
mixing a quantity of a HMFO feed with a quantity of an Activating Gas to give a Feedstock Mixture,
mixing a quantity of Feedstock HMFO, ... with a quantity of Activating Gas mixture to give a feedstock mixture;
mixing a quantity of the pre-treated Feedstock HMFO with a quantity of an Activating Gas mixture to give a Feedstock Mixture;
mixing a quantity of the pre-treated Feedstock HMFO with a quantity of Activating Gas mixture to give a Feedstock Mixture
said HMFO feed complies with ISO 8217 (2017) Table 2 as a residual marine fuel, except said HMFO feed has 1+ Environmental Contaminants selected from the group consisting of: sulfur; vanadium, nickel, iron, aluminum and silicon and combinations thereof, and wherein said 1+ Environmental Contaminants have a combined concentration greater than 0.5% wt.;
wherein the Feedstock HMFO is compliant with ISO 8217:2017 as a residual marine fuel oil, except the Environmental Contaminants content is greater than 0.5% wt. and wherein the Environmental Contaminants are selected from the group consisting of sulfur, vanadium, nickel, iron, aluminum and silicon and combinations thereof,
wherein the Feedstock HMFO is compliant with ISO 8217 (2017) Table 2 as a residual marine fuel, except for: the concentration of the Environmental Contaminates is greater than 0.5 mass % and selected from the group consisting of sulfur, vanadium, nickel, iron, aluminum plus silicon and combinations thereof;
processing the Distressed Fuel Oil Materials in a pre-treatment unit under operative conditions to give a pre-treated Feedstock HMFO, . . . wherein the pre-treated Feedstock HMFO complies with ISO 8217 except for the environmental contaminates including a sulfur content (ISO 14596 or ISO 8754) between the range of 5.0 wt % to 0.50 wt %
contacting the Feedstock Mixture with one or more catalysts under hydrotreating reactive conditions in a Reaction System to form a Process Mixture from said Feedstock Mixture,
contacting the feedstock mixture with 1+ catalysts under reactive conditions to form a Process Mixture, and wherein the reactive conditions are selected to achieve a level of hydrocracking of the Feedstock HMFO of less than 10% of the total mass balance;
contacting the Feedstock Mixture with 1+catalyst materials under reactive conditions sufficient to both: i) decrease the concentration of Environmental Contaminants and ii) minimize the level of hydrocracking to less than about 10% volume
4 catalyst composition
wherein each of said reactor train is configured with at least two reactor vessels in series, and
contacting the feedstock with hydrodemetallization catalyst and hydrodesulfurization catalyst
c 17,18 in one or more reaction vessels under reactive conditions
--
wherein each reactor vessel is independently selected from the group of operational configurations consisting of: dense packed fixed bed trickle reactor; dense packed fixed bed up-flow reactor; ebullated bed three phase up-flow reactor; fixed bed divided wall reactor; fixed bed three phase bubble reactor; fixed bed liquid full reactor, fixed bed high flux reactor; fixed bed structured catalyst bed reactor; fixed bed reactive distillation reactor and combinations thereof, and
10. The process of claim 6, wherein said one or more catalysts is a transition metal heterogeneous catalyst selected from the group consisting of: an ebullated bed supported transition metal heterogeneous catalyst, a fixed bed supported transition metal heterogeneous catalyst, and a combination of ebullated bed supported transition metal heterogeneous catalysts and fixed bed supported transition metal heterogeneous catalysts.
--
--
. . . first reactor vessel catalyst materials selected from the group consisting of hydrodemetallization catalyst, hydro-transition catalyst, inert catalyst materials and combinations thereof; and then . . . . second reactor vessel containing 1+ catalyst materials selected from the group consisting of hydro-transition catalyst, hydrodesulfurization catalyst, inert catalyst materials, and combinations thereof;
16. . . .contacting the Feedstock Mixture with at least one hydrodemetallization catalyst under hydrodemetallization conditions and contacting the Feedstock Mixture with at least one hydrodesulfurization catalyst under hydrodesulfurization conditions such that the combined contacting selectively removes the Environmental Contaminants from the Feedstock HMFO.
17, 18 contacting the feedstock with hydrodemetallization catalyst and hydrodesulfurization catalyst
contacting the Feedstock Mixture with one or more transition metal catalysts under reactive conditions to form a Process Mixture from said Feedstock Mixture4 catalyst composition
wherein said Process Mixture comprises a Product HMFO, by-product hydrocarbons having a boiling point less than 150 F and bulk gases;
wherein the Process Mixture contains one or more Product HMFO liquid components, gaseous components and by-product hydrocarbon,
wherein said Process Mixture is composed of a Product HMFO liquid component, gaseous components and by-product hydrocarbon;
separating Product HMFO liquid components of the Process Mixture from gaseous components and by-product hydrocarbon of the Process Mixture
receiving by fluid communication said Process Mixture in 1+ separation vessel and separating the Product HMFO from the by-product hydrocarbons and the bulk gases and, discharging said Product HMFO from the 1+ separation vessel,
receiving said Process Mixture and separating the one or more Product HMFO liquid components of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture to form a Product HMFO; and
receiving said Process Mixture and separating a Product HMFO liquid component of the Process Mixture from the gaseous components and by-product hydrocarbon components of the Process Mixture and,
receiving said Process Mixture and separating Product HMFO liquid components of the Process Mixture from gaseous components and by-product hydrocarbon components of the Process Mixture and, discharging the Product HMFO.
wherein said Product HMFO complies with ISO 8217:2017 Table 2 as a residual marine fuel. + sulfur less than 0.5 wt %
13 Product HMFO is compliant with ISO 8217:2017 as a residual marine fuel oil + sulfur 0.05% wt. to 0.5% wt.
14. The process of claim 6, wherein said Product Heavy Marine Fu
a Product HMFO [that]complies with ISO 8217 (2017) Table 2 as a residual marine fuel + max contaminant 0.5wt %
2 the Product HMFO complies with ISO 8217: 2017 + sulfur 0.05 wt % to 0.50 wt %.
Additional Art of Record
U.S. Patent No. 10,836,966, US Patent No. 10,604,709 and US Patent No. 11,021,662 claims a similar process using fixed bed reactive distillation with more than one structured packing bed, but fails to claim a second reactor vessels in series with the reactor distillation vessel and in specific stages claimed. Reactive distillation vessels may be used in series; however, the specific instant claims would not be obvious over the claimed limitations in the reference patents.
Conclusion
Any inquiry concerning this communication or earlier communications from the examiner should be directed to Brandi Doyle whose telephone number is (571)270-1141. The examiner can normally be reached Monday-Friday, 8:00 AM - 3:00 PM.
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/BRANDI M DOYLE/Examiner, Art Unit 1771
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