| US 7,462,275 B2 | ||
| Process for conversion of hydrocarbons to saturated LPG and high octane gasoline | ||
| Asit Kumar Das, Faridabad (India); Debasis Bhattacharyya, Faridabad (India); Gadari Saidulu, Faridabad (India); Satayen Kumar Das, Faridabad (India); Bandaru Venkata Hari P. Gupta, Faridabad (India); Ramakrishnan Ramanarayanan, Faridabad (India); Latoor Lal Saroya, Faridabad (India); Konduri Lakshminarayana, Faridabad (India); Marri Rama Rao, Faridabad (India); Vinod Ramchandra Upadhyay, Faridabad (India); Sukumar Mandal, Faridabad (India); Deepa Meghavathu, Faridabad (India); Arumugam Velayutham Karthikeyani, Faridabad (India); Wadharwa Ram Kalsi, Faridabad (India); Arvind Pratap Singh, Faridabad (India); Veena Bansal, Faridabad (India); Ashok Kumar Tiwari, Faridabad (India); Venkatachalam Krishnan, Faridabad (India); Satish Makhija, Faridabad (India); Sobhan Ghosh, Faridabad (India); and Niranjan Raghunath Raje, Faridabad (India) | ||
| Assigned to Indian Oil Corporation Limited, (India) | ||
| Filed on Jul. 20, 2004, as Appl. No. 10/894,341. | ||
| Prior Publication US 2006/0016725 A1, Jan. 26, 2006 | ||
| Int. Cl. C10G 67/00 (2006.01) | ||
| U.S. Cl. 208—97 [208/74; 208/75; 208/76; 208/77; 208/78; 208/113; 208/157] | 19 Claims |
| 1. A process for catalytic conversion of hydrocarbon feed stream having 95% true boiling point less than about 400° C. to
LPG in the range of 30 to 65 wt % of the hydrocarbon feed stream, the said LPG comprising C3 and C4 hydrocarbons, and gasoline
having octane number greater than about 92, said process comprising:
(a) contacting in a riser the hydrocarbon feed stream with hot activated micro-spherical solid fluidizable catalyst composition
consisting of 5 to 40 wt % of medium pore crystalline alumino-silicate, 0 to 10 wt % of “Y” type zeolite, 0 to 5 wt % of non
crystalline acidic material and the remaining being non-acidic component and binder; and
(b) transporting the mixture of hydrocarbon feed stream and the catalyst into a dense bed reactor operating with weight hourly
space velocity (WHSV) in the range of 0.1 to 20 hr−1, hydrocarbon feed stream residence time being greater than 5 seconds and catalyst residence time being greater than or equal
to 60 seconds for cracking the hydrocarbon feed stream at a temperature in the range of 400 to 500° C. and pressure in the
range of 2 to 20 kg/cm2 (g) thereby obtaining LPG comprising C3 and C4 hydrocarbons with olefin content less than 20% (wt/wt) and propane to butane
ratio of more than 2 (wt/wt) and having propane in the range of 50 to 70%;
wherein the hydrocarbon feed stream is substantially devoid of hydrocarbons having less than or equal to 4 carbon atoms and
comprises straight run naphtha (SRN), light cycle oil (LCO), coker naphtha (CN), FCC gasoline (FCCN), mixed naphtha predominantly
containing straight run naphtha (MSN), mixed naphtha containing 50 wt % coker naphtha CN, a feed stream comprising 90 wt %
of MCN and 10 wt % FCCN or mixtures of two or more thereof.
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