LPG.PPT
- 1. Aniruddh Singh ShekhawatAniruddh Singh Shekhawat
- 3. Process Flow Gas to HBJ Line Consumers Gas to Local LPG NAPHTHA SULPHUR SKO C F U Gas Terminal L P G G S U G D U D P D CWU KRU S R U Fractionation of Associated Sour Condensate to Produce LPG & NGL Condensate Fractionation Unit Removal of H2S by Selective Absorption in Methyl Di-ethanol Amine. Gas Sweetening Unit ATF &DIESEL Fractionation of NGL to produce Kerosene & Aromatic Rich Naptha Kerosene Recovery Unit Production of LPG & NAPHTHA from Sweet Gas by Cryogenic Process LPG Recovery Unit Removal of Moisture by Absorption in Tri-ethylene Glycol Gas Dehydration Unit Removal of Liquid Hydrocarbon to make it suitable for transportation through 2300 Km. long HBJ pipe line. Dew Point Depression Unit To receive & Separate Sour Gas & Associated Condensate from Offshore Gas TerminalConversion of Hydrogen Sulphide to Elemental Sulphur for Environmental Protection Sulphur Recovery Unit Sour Gas Sour Cond
- 4. LPG ARN Multi-Component Distillation Drying ChillingDryingFeed Gas DPD Condensate LPG PLANT HGPC HAZIRALPG PLANT HGPC HAZIRA Liquid Gas HP LEAN GAS LP LEAN GAS
- 5. FEED/PRODUCTFEED/PRODUCT LPG Plant Sweet Gas FROM GSU Sweet Gas FROM GSU Condensate FROM DPD Condensate FROM DPD LP Lean Gas LP Lean Gas FUEL GAS LPG HP LEAN GAS ARN PROPANE
- 6. WHAT IS LPGWHAT IS LPG?? LPG is an abbreviation forLPG is an abbreviation for ''LiquifiedLiquified Petroleum GasPetroleum Gas '' This is a general description of PropaneThis is a general description of Propane (chemical formula(chemical formula CC33HH88) and Butane) and Butane (chemical formula(chemical formula CC44HH1010), either stored), either stored separately or together as a mix.separately or together as a mix.
- 7. FEED COMPOSITIONFEED COMPOSITION LPG UNITLPG UNIT COMPONENT FEED GAS CONDANESAT E MOLE % MOLE % CO2 5.34 3.07 C1 80.72 24.29 C2 7.03 11.37 C3 4.2 19.17 iC4 0.86 7.69 nC4 1.06 11.48 iC5 0.29 4.71 nC5 0.33 5.1 C6 0.18 7.5 C7 0 4.1 C8 0 1.14 C9 0 0.3
- 8. Gas Rcpt Gas Dryer C O L D B O X SEP-1 SEP-II LEF Column LPG Column DPD COND REGENERA TION SYSTEM HP LEAN GAS Main Exp - Comp Lean Gas Comp Propane Column REFRIGER ATION SYSTEM SWEET GAS LPG to Storage ARN to Storage FUEL GAS LEF O/H Exp-Comp BLOCK DIAGRAM - LPG To Cold Box Ex LEF O/H Exp- Comp Liquid dryer LP GAS C3
- 9. SECTIONS OF LPG UNITSECTIONS OF LPG UNIT *HP GAS SECTION *LIQUID SECTION *COLUMN SECTION *LP GAS & DRYER REGENERATION *REFRIGERATION SYSTEM
- 10. V 101 GAS DRYER D101 A/B X101A/B GAS FILTERS EX EK101 A/B K 103 A/B CW CW PV 104 COLD BOX E 101 E 103 A/B E 102 A/B E 122 PV 001 PV 002 PV 603 REGN REGN V 102 V 104 V 103 COMP TO CONDANSATE SURGE DRUM GAS FROM GSU FROM V105 TO LEF COLUMN HP GAS SECTION HPGAS TO WRBC COM P P108A/B
- 11. COND. SURGE DRUM V 115 X 102 A/B LIQUID DRYERS D 102 A/B P 108 A/B E 115 STEAM P 106 A/B/C FROM FEED GAS KOD TO FEED GAS HEADER REGENERATION OUTLET REGENERATION INLET TO LEF COLUMN CONDENSATE FROM DPD X103 LIQUID SECTION
- 13. V-111 V-112 V 108 V 109LEFCOLUMN C 101 LPGCOLUMN NAPTHA E 109 E 110 CW P 101 A/B P 102 A/B LV1001 CW E 108 FV1002 FV903 1 REFRIGERATION E106 LP GAS LP STEAM E107 DPD CONDENSATE FROM SEP.-I FROM SEP.-II CONDENSATE FV902 V112 MP STEAM CONDENSATE LPG TO PROPANE COLUMN C102 FLARE P V 1 0 0 1 A / B PIC1001A/B FV1102 COLUMN SECTION
- 14. V 110 P 104 A/B E 111 P103A/B V-112 E 112 V113 LPG E 113 CW 6 CONDENSATE LLP STEAM 26 FEED AS LPG LPG PROPANE PROPANECOLUMN C 103 PROPANE COLUMN CW
- 15. LP GAS TO KCO TO HP LEAN GAS HDR V 106 V 107 E 104 CW K 104 A/B RESIDUE GAS COMPRESSOR E 105 CW PV 802 PV 803 EXP COMP EK 102 PV801 E 123 FURNACE F 101 GAS DRYER D101 A/B LIQUID DRYERS D 102 A/B REGENERATION INLET TO E101 V 105 FROM E101 FROM LEF TOP (V108 ) GAS IN GAS OUT LIQUID IN LIQUID OUT FIC 401 FIC 402 HIC 401 LP GAS & DRYER REGENERATION
- 16. EX EK101A/B COMP PR. 55 Kg/cm2 TEMP- - 300 C PR. 28.5 Kg/cm2 TEMP- - 540 C PR. 35 Kg/cm2 TEMP- 450 C PR. 28.5 Kg/cm2 TEMP- 280 C
- 17. Iso Enthalpic vs Iso- Entropic Process CONSTANT PR. LINESCONSTANT ENTHALPY LINES H1 H2 H3 P1 P3P2 T E M P E N T R O P Y TA TB TC TA - TC Ex.COMP. TA - TB JT V/V TA -TC
- 18. TIC 1202 ACCUMULATOR V117 K105 V118 E106 V119 V120 x xE118 A/ B HIC1201 HIC1203 HIC 1202 FIC 1201 FIC 1202 TIC 1201 LIC 1202 LIC 1201 E119 E120 QUENC H QUENC H REFRIGERATION SYSTEM FOR LEF TOP CONDENSER E106
- 19. LPG SPECIFICATION *DENSITY AT 15 0 C (g/ml) 0.54 *RVP AT 65 0 C (kg/cm2 ) 10.0 (min.) 16.87 (max) *VOLATILITY FOR 95% 0 C +2 (max) BY VOLU. *COPPER STRIPP (01 H r. AT 38 0 C) NOT WORSE CORROSION THAN 1 (a) ASTM * TOTAL VOLATILE SULPHUR 0.02 % (max)
- 20. DESIGN CAPACITYDESIGN CAPACITY MaterialMaterial Design capacityDesign capacity Gas feedGas feed 5.00 MMNCMD5.00 MMNCMD DPD condensateDPD condensate 960 M3 /Day960 M3 /Day LPGLPG 660 TPD660 TPD ARNARN 306TPD306TPD HP Lean gasHP Lean gas 4.22 MMNCMD4.22 MMNCMD LP Lean GasLP Lean Gas 0.54 MMNCMD0.54 MMNCMD
- 21. FEATURES OF LPG UNIT,FEATURES OF LPG UNIT, HAZIRAHAZIRA Gas based plant handles liquid from DPD unit also.Gas based plant handles liquid from DPD unit also. Processes involve production and utilization of veryProcesses involve production and utilization of very low temperatures.low temperatures. Water poses severe problem of gas hydrateWater poses severe problem of gas hydrate formation at low temperatures ,hence the natural gasformation at low temperatures ,hence the natural gas is dried in Gas Driers to reduce the moisture contentis dried in Gas Driers to reduce the moisture content up to 2 ppm level before processing in LPG plant.up to 2 ppm level before processing in LPG plant. Isentropic expansion of gas through turbo expanderIsentropic expansion of gas through turbo expander lowers the gas temperature up to 54lowers the gas temperature up to 5400 C.C. Refrigeration thus produced is utilised in the coldRefrigeration thus produced is utilised in the cold box, the heart of the plant and the condensed liquidbox, the heart of the plant and the condensed liquid is separated out.is separated out. Liquids from separators along with condensate fromLiquids from separators along with condensate from DPD is distilled in two columns to produce LPG &DPD is distilled in two columns to produce LPG & NaphthaNaphtha
- 25. LNG LNG is usually transported by cryogenic ships. With advancement in technology, the size of LNG carrying ships have increased over years. Currently, vessels have capacities of about 138 to 145,000 m3 and designs are underway for capacities of upto 200,000 m3 and more. LNG tankers are double-hulled ships, specially designed and insulated to prevent leakage or rupture in an accident. LNG is stored in a special containment system within the inner hull where it is kept at atmospheric pressure and below 161属C A typical LNG carrier measures about 900 feet in length , 140 feet width and costs about $160 million. From April 2004 commercial supply of re-gasified LNG started from the 5 MMTPA Dahej terminal of Petronet LNG Ltd. Currently many companies are both PSUs and private companies have proposals to import LNG though various ports in the country.
- 26. NATURAL GASNATURAL GAS What is the distinction between CNG, PNG & LNG CNG is natural gas compressed to a pressure of 200 250 kg/cm2 to enhance the vehicle on-board storage capacity. Thus this compressed form of natural gas is used as a fuel for transportation purposes. PNG is Piped Natural Gas supplied homes and establishments. PNG installations contain only a limited quantity of natural gas a low pressure and is much safer compared to LPG which is stored in a cylinder. LNG is liquefied Natural gas cooled to a temperature of below 161属C. It does not contain any other impurities such as oil, particulates, H2S or Oxygen.
- 27. NATURAL GAS What is Natural Gas? A naturally occurring mixture of hydrocarbon and non- hydrocarbon gas found in porous geological formations beneath the earths surface often in association with oil the principal constituent being Methane What is LNG? Liquefied Natural Gas (LNG) is natural gas that has been cooled to the point that it condenses to a liquid which occurs at a temperature of about 161属C at atmospheric pressure. Liquefaction reduces the volume by approximately 600 times, thus making it more economical for transportation
- 28. Comparison of Various ProcessesComparison of Various Processes PropanePropane RefrigerationRefrigeration J T ExpansionJ T Expansion Expasion in Turbo-Expasion in Turbo- ExpanderExpander Different fromDifferent from other twoother two processes. Externalprocesses. External media propanemedia propane cools the gas.cools the gas. Pressure drop inPressure drop in this process isthis process is minimum.minimum. Gas shrinkage rateGas shrinkage rate is 14.33 %is 14.33 % CC44 recovery is 87recovery is 87 %.%. Iso-enthalpic process.Iso-enthalpic process. Lesser amount of coolingLesser amount of cooling than iso-entropic expansionthan iso-entropic expansion over the same pressure drop.over the same pressure drop. High pressure drop,henceHigh pressure drop,hence high power requirement forhigh power requirement for recompression of lean gas forrecompression of lean gas for transportation to consumerstransportation to consumers results in high operating cost.results in high operating cost. Gas shrinkage rate is 8.77Gas shrinkage rate is 8.77 %.%. CC44 recovery is 79.83 %.recovery is 79.83 %. Iso-entropic process.Iso-entropic process. Results in largerResults in larger amount of cooling thanamount of cooling than iso-enthalpic processiso-enthalpic process over the same pressureover the same pressure difference.difference. The work producedThe work produced during expansion isduring expansion is conserved and utilized forconserved and utilized for compression of the leancompression of the lean gas, thus makes it highlygas, thus makes it highly energy efficient.energy efficient. Gas shrinkage rate isGas shrinkage rate is 14.71 %.14.71 %. CC44 recovery % is 94.recovery % is 94.