Naphtha Processing Unit for Sale

Naphtha Splitter Unit built in 2005, consisting of a main splitter column, reboiler, and a feed-bottom exchanger. The unit processes sweet full range naphtha feedstock to separate heavy naphtha (90 °C - 180 °C) from light naphtha (C5 and C6). The E-102 Naphtha Splitter is 45,410 mm T/T with a 4,200 mm internal diameter. 7 barg / full vacuum at 210°C. The C-105 A/B Reboiler is Carbon Steel, 2,382 TT with an 889 mm internal diameter. The shell rated for 13.5 barg / full vacuum at 210°C, tube side is rated for 17.2 barg / full vacuum at 295°C. The C-103 Feed Bottom Exchanger, shell rated 29 barg / full vacuum at 210°C, tube rated 34 barg / full vacuum at 180 °C. Controls and utilities are not included.

Unused naphtha fractionation plant designed to process heavy naphtha from condensate fractionation plants in refineries to produce (N+A) reformed naphtha, diesel and gasoline. The plant is of modular type and is assembled in structure containing platforms, railings and ramp access stairs. All the equipment is mounted on modules, except for the fractionation tower, diesel exhauster, pre-flash tank, direct fire heater and storage tanks. The plant has a service factor of 96.16% (8,328 hours of operation per year). The plant has ABB DCS control system (model 800 xA). The plant equipment was installed but never used. The plant includes the following process sections: (a) Pre-heating and Heating of Heavy Naphtha (b) Fractionation of Heavy Naphtha (c) Obtaining Diesel Product (d) Obtaining Reformed N+A Naphtha (e) Obtaining Gasoline (HGO)

Used 7,500 BPD Naphtha Hydrotreating / Reforming Unit built in 1981. The naphtha ultrafiner / ultraformer unit is designed to convert naptha to a high octane reformate, for use as gasoline base stock, hydrogen and LPG. The ultrafiner removes sulphur from the feed to produce the sweet naphtha charge required by the ultraformer, which then reforms the naphtha to produce high octane material. Both processes are catalytic and operate at a hydrogen concentration to prevent coke forming on the catalyst beds. The feed stream from the pump discharge is combined with make-up hydrogen from the ultraformer and preheated by exchange against ultrafiner rector effluent before entering the ultrafiner reactor charge furnace. From the furnace the stream passes downwards through the catalyst in the ultrafiner reactor where the sulphur compounds in the naphtha are converted to H2S. The ultraformer charge is combined with hot recycle gas and heated in the ultraformer feed/effluent exchanger, before passing to the ultraformer reactor preheat furnace.