An LNG (liquefied natural gas) receiving terminal with C2+ or C3+ separation facility can receive LNG feeds with varying compositions, meet stringent calorific value export gas specifications, and decrease capital and operating costs. A study shows that process schemes for extracting C2 or C3 from rich imported LNG are feasible, effective, and economical. A minor required change in typical LNG receiving terminal equipment includes modification of the sendout pumps' casing to a higher pressure rating; however, no additional compression is required. Compared to a system that requires sendout gas compression or an inert-gas injection system to dilute the sendout gas, C2+ or C3+ separation can reduce the capital investment by at least 40 % and decrease operating costs. The cost-effective designs include additional facilities that are not standard in most receiving terminals. This includes a separation system, which consists primarily of one or two fractionation columns with plate-and-fin or shell-and-tube exchangers for overhead condensers. The designs use low-temperature LNG as a cooling medium for the column overhead to achieve an economic separation. These designs require no gas compression because they use LNG as a refrigerant in a direct-contact condenser; this condenses enriched C1 vapor from the column overhed to produce a lean LNG for liquid pumping. The designs also use existing vaporizers to vaporize column feed.
Cost-effective design reduces C2 and C3 at LNG receiving terminals
Ein kosteneffektives Design zur C2+- und C3+-Trennung bei LNG-Lieferterminals
Oil and Gas Journal ; 101 , 21 ; 50-53
2003
4 Seiten, 2 Bilder, 1 Quelle
Aufsatz (Zeitschrift)
Englisch
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