Anthony N Go

20100305381, Dec 2, 2010

May 5, 2010

12/774319

Anthony Go - Houston TX, US
Dana Lynn Pilliod - League City TX, US
John R. Porter - Friendswood TX, US

C07C 7/12

585826

A process for separating a product from a multicomponent feedstream to an adsorption apparatus or system. The apparatus or system may comprise a moving-bed or a simulated moving-bed adsorption means. The product comprises at least one organic compound, such as an aryl compound with alkyl substitutes. In embodiments the conduits used to supply the feedstream to the apparatus or system are flushed with media of multiple grades. In embodiments the process achieves improvements in one or more of efficiency of adsorption separation, capacity of adsorption apparatus systems, and purity of product attainable by adsorption process.

20130144097, Jun 6, 2013

Nov 14, 2012

13/676813

Timothy P. Bender - Houston TX, US
John W. Rebeck - Katy TX, US
Rimas V. Vebeliunas - Houston TX, US
John R. Porter - Friendswood TX, US
Anthony Go - Houston TX, US
Larry L. Iaccino - Seabrook TX, US
Glenn C. Wood - Houston TX, US

ExxonMobil Chemical Patents Inc. - Baytown TX

C07C 2/64
C07C 5/22
B01J 19/00

585254, 422187, 585304

In a process for producing para-xylene, a naphtha feed is reformed under conditions effective to convert at least 50 wt % of the naphthenes in the naphtha feed to aromatics, but to convert no more than 25 wt % of the paraffins in the naphtha feed, and thereby produce a reforming effluent. A first stream containing benzene and/or toluene is removed from the reforming effluent and is fed to a xylene production unit under conditions effective to convert benzene and/or toluene to xylenes. In addition, a second stream containing C8 aromatics is removed from the reforming effluent and is fed, together with at least part of the xylenes produced in the xylene production unit, to a para-xylene recovery unit to recover a para-xylene product stream and leave a para-xylene-depleted C8 stream. At least part of para-xylene-depleted C8 stream is then fed to a xylene isomerization unit effective to isomerize xylenes in para-xylene-depleted stream back towards an equilibrium mixture of xylenes and thereby produce an isomerization effluent. The isomerization effluent is then recycled to the para-xylene extraction unit.

20220195309, Jun 23, 2022

Jun 12, 2020

17/595344

- Baytown TX, US
Bryan A. Patel - Jersey City NJ, US
Randolph J. Smiley - Hellertown NJ, US
Lawrence R. Gros - Katy TX, US
Anthony Go - Houston TX, US
Saurabh S. Maduskar - Houston TX, US
Melissa D. Foster - Humble TX, US
Philippe Laurent - Houston TX, US

C10G 1/10
C10G 9/36
C10B 49/22
C10B 53/07

Systems and methods are provided for integration of a reactor for polyolefin pyrolysis with the effluent processing train for a steam cracker. The polyolefins can correspond to, for example, polyolefins in plastic waste. Integrating a process for polyolefin pyrolysis with a steam cracker processing train can allow a mixture of polymers to be converted to monomer units while reducing or minimizing costs and/or equipment footprint. This can allow for direct conversion of polyolefins to the light olefin monomers in high yield while significantly lowering capital and energy usage due to integration with a steam cracking process train. The integration can be enabled in part by selecting feeds with appropriate mixtures of various polymer types and/or by limiting the volume of the plastic waste pyrolysis product relative to the volume from the steam cracker(s) in the steam cracking process train. By selecting plastic waste and/or other polyolefin sources with an appropriate mixture of polyolefins as the feedstock, the resulting polyolefin pyrolysis product can be separated in a steam cracking process train to produce separate fractions for various polymer grade small olefin products.

20210122688, Apr 29, 2021

Apr 19, 2018

16/605387

- Baytown TX, US
Todd E. Detjen - Bellaire TX, US
Mayank Shekhar - Houston TX, US
Anthony Go - Houston TX, US

C07C 7/08
C07C 5/27
C07C 29/48

Systems and methods are provided for integration of an aromatic formation process for converting non-aromatic hydrocarbon to an aromatic product and subsequent methylating of a portion of the aromatic product to produce a methylated product, with improvements in the aromatic formation process and/or the methylation process based on integrating portions of the secondary processing trains associated with the aromatic formation process and the methylation process. The aromatic formation process and methylation process can be used, for example, for integrated production of specialty aromatics or gasoline blending components.

20210040016, Feb 11, 2021

Mar 15, 2019

16/979751

- Baytown TX, US
Wenyih F. Lai - Bridgewater NJ, US
Anthony Go - Houston TX, US

C07C 2/86
C07C 5/27
C10L 1/06
C10L 10/10
B01J 29/70
B01J 35/10
B01J 29/18

Disclosed is a process for producing mixed xylenes and C hydrocarbons in which an aromatic hydrocarbon feedstock comprising benzene and/or toluene is contacted with an alkylating agent comprising methanol and/or dimethyl ether under alkylation conditions in the presence of an alkylation catalyst to produce an alkylated aromatic product stream comprising the mixed xylenes and C hydrocarbons. The mixed xylenes are subsequently converted to para-xylene, and the C hydrocarbons and its components may be supplied as motor fuels blending components. The alkylation catalyst comprises a molecular sieve having a Constraint Index in the range from greater than zero up to about 3. The molar ratio of aromatic hydrocarbon to alkylating agent is in the range of greater than 1:1 to less than 4:1.

20200181042, Jun 11, 2020

Feb 9, 2017

16/074220

- Baytown TX, US
- Atlanta GA, US
Jeevan S. ABICHANDANI - Houston TX, US
Dana L. PILLIOD - League City TX, US
John R. PORTER - Friendswood TX, US
Anthony GO - Houston TX, US
Sankar NAIR - Atlanta GA, US
Ke ZHANG - Medford MA, US

C07C 5/27
C07C 7/12
C07C 7/04
C07C 7/00
B01J 20/22
B01J 20/16
B01J 29/70
B01J 35/10
B01J 35/00
B01D 15/18
B01D 3/14

Para-xylene is separated from a mixture of xylenes and ethylbenzene by a separation process. An ortho-selective adsorbent is used to reduce the ortho-xylene concentration of the xylenes, prior to contact of the xylenes and ethylbenzene with a para-selective adsorbent. The stream rich in ortho-xylene may be isomerized in the liquid phase to increase the amount of para-xylene therein. The para-xylene-depleted stream may be treated in the vapor phase to remove the ethylbenzene and then subjected to isomerization in the liquid phase to produce a stream having a higher than equilibrium amount of para-xylene.

20190127294, May 2, 2019

Dec 21, 2018

16/228892

- Baytown TX, US
Paul F. Keusenkothen - Houston TX, US
Machteld M. Mertens - Boortmeerbeek, BE
Anthony Go - Houston TX, US

C07C 2/76
C10G 35/06
B01J 29/40
B01J 29/44
B01J 29/46
B01J 29/90
B01J 37/08
B01J 38/04

The invention relates to catalysts and their use in processes for conversion of hydrocarbon feedstock to a product comprising single-ring aromatic hydrocarbons having six or more carbon atoms, to the methods of making such catalysts, to processes for using such catalysts, and to apparatus and systems for carrying out such processes. One of more of the catalysts comprise a crystalline aluminosilicate having a Constraint Index in the range of 1 to 12, a first metal and/or a second metal, and at least one selectivating agent, such as, for example, an organo-silicate.

20180215684, Aug 2, 2018

Jul 29, 2016

15/747951

- Baytown TX, US
- Atlanta GA, US
Dana L. PILLIOD - League City TX, US
Robert G. TINGER - Friendswood TX, US
Anthony GO - Houston TX, US
Ke ZHANG - Medford MA, US
Sankar NAIR - Atlanta GA, US
Jason GEE - Houston TX, US
David SHOLL - Marietta GA, US

C07C 7/12
C07C 7/00
C07C 7/04
C07C 5/27
B01D 15/18
B01D 3/14

Para-xylene is separated from a mixture of C8 aromatics using a simulated moving bed (SMB) adsorption process, wherein a MOF is used as an adsorbent and an alkane or alkene having 7 or less carbon atoms, such as hexane or heptane is used as desorbent. Because of the difference in boiling points of a hexane or heptane desorbent as compared to conventional desorbents such as toluene or para-diethylbenzene, less energy is required to separate hexane or heptane from C8 aromatics by distillation than the energy required to separate toluene or diethylbenzene from C8 aromatics by distillation.