Deep Panuke Project Description - Encana

For the M&NP Option, the export gas will be “on specification” sales gas meeting the hydrocarbondewpoint and water content requirements for the M&NP pipeline. As a result, there is no onshoretreatment required. The sales gas will be routed to shore near Goldboro in a new 560 mm [22 inch]pipeline with a connection into the existing M&NP pipeline. Onshore facilities are related tometering/quality measurement and isolation valve requirements only. The liquids will be treatedoffshore and used as fuel. Currently it is estimated that there will be no surplus condensate producedbeyond fuel usage. To allow flexibility in times of maintenance and/or operational issues, condensatewill be commingled with the acid gas and re-injected for disposal.For the SOEP Subsea Option, the export gas and condensate will be commingled and routed to theSOEP 660 mm [26 inch] pipeline and routed to the existing SOEP Goldboro gas plant. At Goldboro, thegas and liquids will be separated and the gas further processed into sales gas by SOEP and shipped viathe existing M&NP pipeline to market. The liquids will be routed to the SOEP Point Tupper liquidsplant for processing and sale.2.4.1.1 SeparationThe well fluids will be processed through the production or test separator for separation of the gas,condensate, and water.2.4.1.2 MeteringThe Deep Panuke production facilities will adhere to the applicable regulations and the Canada-Newfoundland Offshore Petroleum Board (CNOPB)/CNSOPB Measurement Guidelines, October 2003.2.4.1.3 Amine SweeteningThe amine sweetening system, which uses methyldiethanolamine (amine), is designed to remove theH 2 S contained in the raw gas. The removal of the H 2 S and CO 2 from raw gas results in a waste acid gasstream predominantly containing H 2 S and CO 2 . The H 2 S content of the raw gas during the life of theProject will vary. The amine sweetening system is designed to operate safely over the expectedvariation of H 2 S content in the raw gas.The Deep Panuke gas contains up to 3.5 mole % CO 2 and approximately 1,800 ppm H 2 S. The aminesweetening unit is designed to be fed with gas that contains up to 2,500 ppmv of H 2 S and up to 3.5 mole% CO 2 to provide some operational design flexibility. The facility metallurgical design will be for 3,000ppmv of H 2 S and 4.0 mole % CO 2 to provide some metallurgical design flexibility. The sales gasspecification requires the H 2 S content to be a maximum of 6 mg/m 3 (approximately 4 ppmv) and 3.0mole % CO 2 . The current design basis unit outlet is for an H 2 S level of 2 ppmv and CO 2 at 2.8 mole %.Deep Panuke Volume 4 (Environmental Assessment Report)• November 2006 2-33