Hydrocarbon Recovery. Chapter 12 Based on presentation by Prof. Art Kidnay

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1 Hydrocarbon Recovery Chapter 12 Based on presentation by Prof. Art Kidnay

2 Reasons for Hydrocarbon Recovery Field Operations Reduce liquid content of high GPM gases in gathering systems Eliminate or reduce potential for condensation (dew-pointing) Reduce Btu content of gas for use in engines (fuel conditioning) Plant Operations Reduce Sales gas Btu content to spec (950 to 1150 Btu/scf) Eliminate possible condensation Recover valuable C 2+ liquids 2

3 Plant Block Schematic 3

4 Topics Fundamentals Retrograde Condensation Process Components Refrigeration System Turboexpansion Heat exchange Gas-Liquid Separators Fractionation Recovery Processes Dew Point Control and Fuel Conditioning Low C2+ Recovery High C2+ recovery 4

5 Fundamentals

6 Retrograde Condensation B C Pressure, Psia Liquid A Vapor Temperature, F 6

7 Rich Gas Phase Diagram 7

8 Rich Gas Phase Diagram 8

9 Operating Conditions Depend on Type of NGL Recovery 9

10 Process Components

11 External Refrigeration When inlet pressures to Hydrocarbon Recovery are too low to provide required cooling by expansion we can obtain additional refrigeration by: Compressing inlet gas to higher pressure Compressing propane in refrigeration cycle Compressing propane is usually the best choice 11

12 Basic Refrigeration System Compressor Condenser Suction Drum Receiver J-T Valve Chiller/ Evaporator 12

13 Refrigeration cycle Compressor B Condenser C Suction Drum Receiver A D J-T Valve Chiller/ Evaporator Pressure C B D * A 13

14 1 Stage C 3 Refrigeration System Compressor 250 Psia Condenser Suction Drum J-T Valve Receiver ~120 F 240 Psia Chiller/ Evaporator -40 F, 16 Psia 14

15 Refrigeration cycle C B D A 15

16 2 Stage C 3 Refrigeration System 60 Psia 250 Psia Condenser JT-Valve - 40 F 16 Psia 25 F 62 Psia Interstage Economizer 25 F 62 Psia Chiller/ Evaporator Receiver ~120 F 240 Psia JT-Valve Chiller / Evaporator -40 F, 16 Psia JT-Valve 16

17 2 Stage C 3 Refrigeration System 60 Psia 250 Psia Condenser - 40 F 16 Psia 25 F 62 Psia Interstage Economizer JT-Valve JT-Valve Receiver ~120 F 240 Psia Chiller / Evaporator -40 F, 16 Psia 17

18 Refrigeration cycle C B D A 18

19 Benefits of Staging Number of Stages Reduction in Compression Power 0 19% 23% Reduction in Condenser Duty 0 8% 10% Condenser Temp = 100 o F Chiller Temp = -40 o F 19

20 Turboexpanders Provide Maximum possible cooling Work which can drive compressors Operate Over wide temperature range At high speeds, > 15,000 rpm Require clean gas Can handle up to 50 wt % liquid formation provided droplet size less than 20 μm 20

21 21

22 Turboexpander Cutaway Mafi Trench Compressor Expander 22

23 Recovery Processes

24 Recovery Processes Dew Point Control and Fuel Conditioning High recovery not needed Operating temperatures ~0 o F for fractionation Low C 2+ Recovery < 60% C 2+ recovery needed Operating temperatures ~ -35 o F for fractionation High C 2+ recovery ~ 90% C 2+ recovery needed Operating temperatures ~ -165 o F for fractionation 24

25 Dew Point Control and Fuel Conditioning Traditional technology Low Temperature Separators (LTS or LTX) Standard technology (>60 years old) Newer technologies Membrane System Newer technology (~10 years old) Twister Newest technology (~5 years old) 25

26 Low Temp Separator with Glycol Injection 26

27 Membrane for Fuel Conditioning 27

28 Twister Modular, flow dependent Depends upon pressure ratio, ΔP ~ 20 to 30% Slip gas is 10 to 15% Used for dehydration and liquids removal Is being tested in subsea application _How_Does_It_Work.pdf 28

29 Low C 2+ Recovery Two major processes Refrigerated Lean Oil Lean Oil Absorption first process for liquids recovery Existing plants now use refrigerated system Refrigerated Process Simpler than Lean Oil process Lower recoveries 29

30 Refrigerated Process 30

31 Effect of Composition on C 3+ Recovery 90 C 3 + Recovery, % GPM 5 GPM 3 GPM Process Temperature, F 31

32 Recovery Efficiency of C 2 and C GPM 5 GPM C 3 Recovery, % GPM 3 GPM 5 GPM 20 3 GPM C Process Temperature, F 32

33 Refrigerated Lean Oil 33

34 High C 2+ Recovery Requires cryogenic separation Processes involve: Propane refrigeration (unless high inlet gas pressure) Multipass heat exchangers (gas-gas) Expansion, turbo and JT Demethanizer column Two processes: 1 st Generation simplest Gas Subcooled Process (GSP) more efficient, higher recoveries and commonly used 34

35 Considerations for Cryogenic Distillation 35

36 1 st Generation Cryo Process 36

Brazed Aluminum Heat Exchanger Cold Box http://hub.globalccsinstitute.

37 Brazed Aluminum Heat Exchanger Cold Box 37

38 GSP Schematic 38

39 Effect of Inerts on Max C 2 Recovery 100 Maximum Ethane Recovery, % GPM 3.0 GPM 5.0 GPM 8.0 GPM Nonhydrocarbon Content, mol % 39

40 Summary

41 Summary Primary liquids production from cold separation Produced gas at dew point condition at last conditions in contact with hydrocarbon liquid Lower liquid content of produced gas has a lower dew point requiring lower temperatures Propane refrigeration loop Typical low temperatures to -40 o F Intermediate pressures reduce compression power & can make chilling temperatures about 10 o F 41

Process Simulation and Optimization of Cryogenic Operations Using Multi-Stream Brazed Aluminum Exchangers

Page 1 of 12 Process Simulation and Optimization of Cryogenic Operations Using Multi-Stream Brazed Aluminum Exchangers JOHN C. POLASEK, Bryan Research & Engineering, Inc., Bryan, Texas STEPHEN T. DONNELLY,