The onshore section of the 6, 7 & 8 project consists of a huge refinery capable of refining 80 million cubic meters of sour gas, condensates, water and impurities into the products mentioned in the table describing the products. The major units of the gas plant are as follows:

• Reception Facilities: The reception facilities are common to phases 6, 7 & 8. This unit includes a pig receiver and manifold section installed at the outlet of each sub-sea-pipeline. The production fluids entering the slug catcher are separated into three physical phases: gas, liquid hydrocarbons and glycolated water.
• High Pressure (HP) Separators: There are two HP Separators for each phase. Gas from each pressure letdown station goes to two HP separators operating in parallel, each being a gas / liquid separator. The gas from each separator is sent to its dedicated gas treatment train for further processing and the excess gas is sent to the flare. Liquid produced in the HP separators is routed to the Condensate Stabilisation Unit under level control.
• Gas Dehydration: The Gas Dehydration Unit is designed to process the sour wet gas leaving HP separators in order to produce a dry sour gas stream. The dry gas is then sent to the NGL Extraction.
• NGL Extraction and Fractionation: Dry sour gas entering the unit is cooled in a series of gas/gas, NGL/gas exchangers and propane refrigerant chilling. The feed flows to the expander suction drum, which provides phase separation between gas and liquid. The liquid goes to the Deethaniser feed and the vapour phase is fed to the Turbo Expander. Liquids recovered via the Low Temperature Separator are used as reflux to the Deethaniser Column.
• Export Gas Booster Compressor: Dry gas streams from the NGL Extraction and Fractionation Units of the six gas trains are combined and entered into the Export Gas Booster Compressor Unit, which is common to all three phases. There are four parallel compression trains, three on-line and one spare. Each train consists of a suction drum, gas turbine-driven compressor and an air-cooled after-cooler. The product gas then flows to the export pipeline.
• Condensate Stabilization: The purpose of the Condensate Stabilization Unit is to reduce the vapor pressure of the hydrocarbon condensate so that it meets the product RVP specification. Liquids separated in the slug catchers and HP separators of each phase are sent to the three trains of the Condensate Stabilization Unit. The feed is preheated by the Condensate Feed Exchanger. The Flash gas from the separator goes to the second stage of off-gas compression. The glycolated water phase is sent to the MEG Recovery Unit. The hydrocarbon liquid is pumped via a Desalter to the Condensate Stabilizer Column.
• MEG Recovery: MEG solution is injected at the offshore platforms to inhibit the formation of hydrates and corrosion in the sub-sea-pipelines. The feed to the MEG Unit is the combined glycolated water collected from the Condensate Stabilization Unit. The glycolated water is filtered to remove suspended solids and entrained hydrocarbons. The MEG is regenerated and the extracted water is sent to the Sour Water Stripper, with the regenerated MEG being sent to the Lean MEG Storage Tank.
• Sour Water Stripper: The incoming liquids are fed to the Sour Water Stripper Feed Drum which is a three phase separator. Flash gas is sent to the incinerator. Hydrocarbon liquids are pumped to the Off-spec Condensate Tank and the sour water phase is pumped to the Stripper which has a steam-heated re-boiler and total reflux. The acid gas from the Sour Water Stripper will be incinerated.
• LPG Treating Unit: Propane from the Depropaniser is sweetened by counter-current contact with a lean solution of amine in a vertical absorber. Propane is then treated with a caustic soda solution to remove remaining sulphur compounds such as mercaptans. The propane finally goes to a molecular sieve (Moisture Separator) drying section and the resulting product, meeting the required specifications, is sent to the LPG Storage facilities. Butane from the Debutaniser is treated with a caustic soda solution to remove sulphur compounds such as mercaptans. The butane then goes to a molecular sieve drying section with the resulting product, meeting required specifications, is sent to the LPG Storage facilities.
• Condensate Storage: Four 75,000 cubic meters floating roof tanks are provided for condensate storage. The total capacity of the tanks is equivalent to approximately fifteen days production. Condensate products flows by gravity to existing NIOC loading pumps and from there the flows to tankers via a metering skid either to an existing or to a new CALM (a floating loading facility) buoy, located respectively 3 km and 6 km offshore.
• LPG Storage: There are two 55,000 cubic meter Propane Storage Tanks and two 40,000 cubic meters Butane Storage Tanks. Propane is cooled against propane refrigerant by a series of three chillers and then sent to storage tanks. Butane is cooled against propane refrigerant in a series of two chillers and then sent to storage tanks. Propane and butane products are stored in double-wall, full containment, refrigerated tanks, each tank having a carbon steel inner tank and a concrete outer tank and dome.

• Utilities: The main parts include: HP/LP Steam Generation and Distribution, Power Distribution, Emergency Power Generation, Sea Water Supply, Cooling Water, Desalinated Water Supply, Demin/Potable/Plant Water Supply and network, Fire Water System, Instrument and utilities Air Supply and Distribution, Nitrogen Supply and Distribution, Fuel Gas Distribution and effluent Treatment
• Control System: The South Pars plant will be controlled from the Central Control Room (CCR) in the main control building. The plant will be operated from the CCR and the operation of systems such as the Export Gas Compressors and the jetty can be performed from the Local Control Room (LCR).