US 11,713,424 B2
Use of Aromax® catalyst in sulfur converter absorber and advantages related thereto
Ryan W. Snell, Jubail Industrial (SA); Scott G. Morrison, Kingwood, TX (US); Vincent D. McGahee, Kemah, TX (US); Xianghong Hao, Kingwood, TX (US); and Gabriela Alvez-Manoli, Kingwood, TX (US)
Assigned to Chevron Phillips Chemical Company, LP, The Woodlands, TX (US)
Filed by Chevron Phillips Chemical Company LP, The Woodlands, TX (US)
Filed on Feb. 14, 2018, as Appl. No. 15/896,507.
Prior Publication US 2019/0249094 A1, Aug. 15, 2019
Int. Cl. C10G 61/00 (2006.01); C10G 61/06 (2006.01); C10G 35/04 (2006.01); C10G 45/02 (2006.01); C10G 69/08 (2006.01); B01D 53/14 (2006.01); C10G 59/02 (2006.01); B01J 29/62 (2006.01); B01J 37/02 (2006.01); C10G 61/02 (2006.01)
CPC C10G 61/06 (2013.01) [B01D 53/1468 (2013.01); B01J 29/62 (2013.01); B01J 37/0201 (2013.01); C10G 35/04 (2013.01); C10G 45/02 (2013.01); C10G 59/02 (2013.01); C10G 61/02 (2013.01); C10G 69/08 (2013.01); B01D 2257/304 (2013.01); C10G 2300/202 (2013.01); C10G 2300/207 (2013.01); C10G 2300/4006 (2013.01); C10G 2300/4031 (2013.01); C10G 2300/70 (2013.01); C10G 2300/701 (2013.01); C10G 2400/30 (2013.01)] 20 Claims
OG exemplary drawing
 
1. A process for operating a reforming system, the process comprising:
operating a reforming section, wherein the reforming section comprises a plurality of reactors, and wherein each of the plurality of reactors contains a reforming catalyst capable of catalyzing the conversion of at least a portion of the hydrocarbons in a treated hydrocarbon stream into a reactor effluent comprising aromatic hydrocarbons, wherein the reforming catalyst comprises at least one Group VIII metal and a zeolitic support; and
operating a sulfur guard bed (SGB) to remove sulfur and sulfur-containing hydrocarbons from a hydrocarbon feed to provide the treated hydrocarbon stream, wherein the SGB comprises
1) A volume from about 16 vol. % to about 30 vol. % of the volume of a total reforming catalyst within the plurality of reactors within the reforming section and operable to remove sulfur, and sulfur-containing hydrocarbons from a hydrocarbon feed to provide the treated hydrocarbon stream,
2) at least a layer of a SGB catalyst and a layer of an iron trap material having a porosity of greater than or equal to about 0.2 cc/g and located downstream of and adjacent to the layer of the SGB catalyst and operable to remove particulate iron from the hydrocarbon feed, where the SGB catalyst and the reforming catalyst are the same and capable of producing hydrogen sulfide from sulfur-containing hydrocarbons and hydrogen, and
3) an inlet line to introduce the hydrocarbon feed into the SGB and an outlet line to remove the treated hydrocarbon stream from the SGB;
monitoring a SGB endotherm, wherein the SGB endotherm is the difference between the temperature of a hydrocarbon feed introduced to the SGB via the inlet line and the temperature of the treated hydrocarbon in the SGB outlet line; and
wherein each reactor of the plurality of reactors of the reforming section is operated at a higher operating temperature than an operating temperature of the SGB, wherein the operating temperature of the SGB is greater than or equal to 800° F. (426.7° C.) and wherein the treated hydrocarbon stream comprises at least one aliphatic hydrocarbon, at least one aromatic hydrocarbon, and hydrogen at a ratio of 1:1:2.