Seminar Kerja Praktek SIZING PIPE of N2 GASES STREAM from CP-53 and MPN as OIL LUBRICATING SYSTEM SEALING at ST-18

Seminar Kerja Praktek

Aisya Morina Haque2313 030 098 Fanina Aulia Rachma2313 030 052PT. LINDE GRESIKPT. Gresik Power Indonesia (PT. GPI) dan PT. Gresik Gases Indonesia (PT. GGI) berlokasi di Desa Roomo, Kecamatan Manyar, Kabupaten Gresik, Jawa Timur. Dengan jenis kegiatan yaitu Industri Pembangkit Tenaga Listrik dan Gas Industri.

Product Low Pressure Gas Oxygen (LPGO) High Pressure Gas Oxygen (HPGO)Gas NitrogenLiquid Oxygen (LOX)Liquid Nitrogen (LIN)Liquid Argon (Lar)Air Separation Unit

Proses ASU

TUGAS KHUSUSSIZING PIPE of N2 GASES STREAM from CP-53 and MPN as OIL LUBRICATING SYSTEM SEALING at ST-18INTRODUCTIONOn 2014, ASU steam turbine (ST-18) has experienced oil leaking many times and one of fire incident caused by ST-18 oil leak ever happened also on 2014.

INTRODUCTIONAn investigation has been conducted and it was found that during this steam turbine 18 has been in operation without any seal gas introduced to its oil system.OBJECTIVETo prevent oil leak and fires incident happening again, a modifications will be made at CP-53 discharge vent line and nitrogen medium pressure (MPN) system to provide seal gas to steam turbine 18 oil system.

Whereas the purpose of this study are DETERMINE THE SIZE OF PIPE that will be used for N2 gases stream from CP-53 and MPN as ST-18 Oil Lubricating System Sealing and its installation.Initial ConditionCompressor CP-53

Pressure : 5 barMPN

Pressure : 4,6 barST-18 Sealing

Pressure : 3,005 bar

Calculating Method

Calculating diameter size of pipe that will be used is also using calculation of pressure drop from source into a goal. On calculating, this study use CHEMCAD software. Using Chemcad is intended to allow more efficient computation, because the process is using TRIAL and ERROR method from the smallest pipe size.

Pre-CalculatingDetermine Coeficient Flow from Technical Specification of RegulatorVelocity Gas : 10 m/sMax Flow in 0.5 inch pipe : 720 ft3/h (12 scfm)Inlet Pressure (Pi) : 159,54 Psia (10 barg)Outlet Pressure (Po) : 114,57 Psia (6,9 barg)Pressure Drop (dp): 44,97 Psia (dp = Pi-Po)Temperature (T): 32 F (0o C) Coeficient Flowrate (Cv) ?

Determine Flowrate (Q) from Coefficient Flow (Cv)Velocity Gas: 10 m/sCoefficient Flowrate: 0.163Inlet Pressure (Pi) : 87,02 Psia (5 barg)Outlet Pressure (Po): 65,26 Psia (3,5 barg)Pressure Drop (dp): 21,76 Psia (dp = Pi-Po)Temperature (T): 32 F (0o C)Flowrate (Q) ?

Input Chemcad from CP-53Temperature: 40CPressure: 6 baraTotal Flow: 10,17 stdV m3/hMole Fraction Nitrogen: 1Pipe Diameter: 0,5 inPipe Schedule: 40Pipe Length: 51,42 m

Elevation: 6,96 mPipe Material : Commercial SteelBall Valve: 3Swing Check: 1Elbow 90 deg: 15Tee: 1Simulating N2 stream from CP-53 by ChemCad

Input Chemcad from MPNTemperature: 40CPressure: 5,6 baraTotal Flow: 10,17 stdV m3/hMole Fraction Nitrogen: 1Pipe Diameter: 0,5 inPipe Schedule: 40Pipe Length: 39,52 m

Elevation: 6,96 mPipe Material: Commercial SteelBall Valve: 3Swing Check: 1Elbow 90 deg: 15Tee: 1

Simulating N2 stream from MPN by ChemCad

ResultThe ChemCad simulation for N2 gases stream from CP-53 shows the final pressure bigger than 3,5 bar, which one is 4,9647 bar of pressure. This shows that the simulated trial suit the demand of process needed. THANK YOU