A slug catcher is a piece of process equipment (typically a pressure vessel or set of pipes) that is located at the outlet of production flowlines or pipelines, prior to the remaining production facilities.
Location of Slug Catcher and Production Separator
Combined Slug Catcher and Production Separator

Slug catchers are used in both oil/gas multiphase production systems and in gas/condensate systems to mitigate the effects of slugs, which are formed due to terrain, pipeline operation in the slug-flow regime, or pigging. A slug catcher is generally not needed for single-phase liquid lines such as treated oil or produced water because slug flow is not encountered in single-phase operation; however, the need for slug catchers should be evaluated if pigging is expected.

Slug Catcher Design Process

The goal of slug catcher design is to properly size the slug catcher for the appropriate conditions. The process consists of the following steps:

  • Determine slug catcher functions.
  • Determine slug catcher location.
  • Select preliminary slug catcher configuration.
  • Compile design data.
  • Establish design criteria.
  • Estimate slug catcher size and dimensions.
  • Review for feasibility; repeat as necessary.

Slug Catcher Functions

The slug catcher functions may be summarized as follows:

  • Process stabilization;
  • Phase separation;
  • Storage.

Each slug catcher can serve one or more functions, and each function is detailed in the following sections.

Process Stabilization

Process stabilization is the primary purpose of the slug catcher. In a typical steady-state operation, multiphase production fluids from the flowline enter the production facilities at constant temperature, pressure, velocity, and flow rate. Process control devices such as pressure control valves and level control valves are used to maintain steady operating conditions throughout the process facilities. During non-steady-state conditions, such as start-up, shutdown, turndown, and pigging, or when slugging during normal operation is expected, the process controllers alone may not be able to sufficiently compensate for the wide variations in fluid flow rates, vessel liquid levels, fluid velocities, and system pressures caused by the slugs.

A slug catcher provides sufficient space to dampen the effects of flow rate surges in order to minimize mechanical damage and deliver an even supply of gas and liquid to the rest of the production facilities, minimizing process and operation upsets.

Phase Separation

The second main function of the slug catcher is to provide a means to separate multiphase production fluids into separate gas and liquid streams in order to reduce liquid carryover in the gas stream and gas re-entrainment in the liquid stream. Gas/liquid separation also occurs, but the efficiency of separation is usually not sufficient to meet oil and gas product specifications. The gas stream may need additional treating to remove entrained liquids prior to treating, compression, or flaring. The liquid may need additional treating for gas/oil/water separation and crude stabilization.

Storage

Slugs that result from pigging can often be significantly larger than terraininduced slugs or slugs formed while operating in the slug-flow regime, particularly for gas/condensate systems with long flowlines or pipelines. In these situations, the condensate processing and handling systems may not be sized to quickly process the large slug volume that results from pigging. The slug catcher then acts as a storage vessel to hold the condensate until it can gradually be metered into the process or transported to another location.

References

[1] R.C. Reid, J.M. Prausnitz, T.K. Sherwood, The Properties of Gases and Liquids, third ed., McGraw-Hill, New York, 1977.

[2] K.S. Pedersen, A. Fredenslund, P. Thomassen, Properties of Oils and Natural Gases, Gulf Publishing Company (1989).

[3] T.W. Leland, Phase Equilibria, Fluid, Properties in the Chemical Industry, DECHEMA, Frankfurt/Main, 1980. 283–333.

[4] G. Soave, Equilibrium Constants from a Modified Redilich-Kwong Equation of State, Chem. Eng. Sci vol. 27 (1972) 1197–1203.

[5] D.Y. Peng, D.B. Robinson, A New Two-Constant Equation of State, Ind. Eng. Chem. Fundam. vol. 15 (1976) 59–64.

[6] G.A. Gregory, Viscosity of Heavy Oil/Condensate Blends, Technical Note, No. 6, Neotechnology Consultants Ltd, Calgary, Canada, 1985.

[7] G.A. Gregory, Pipeline Calculations for Foaming Crude Oils and Crude Oil-Water Emulsions, Technical Note No. 11, Neotechnology Consultants Ltd, Calgary, Canada, 1990.

[8] W. Woelflin, The Viscosity of Crude Oil Emulsions, in Drill and Production Practice,, American Petroleum Institute vol. 148 (1942) p247.

[9] E. Guth, R. Simha, Untersuchungen u¨ber die Viskosita¨t von Suspensionen und Lo¨sungen. 3. U¨ ber die Viskosita¨t von Kugelsuspensionen, Kolloid-Zeitschrift vol. 74 (1936) 266–275.

[10] H.V. Smith, K.E. Arnold, Crude Oil Emulsions, in Petroleum Engineering Handbook, in: H.B. Bradley (Ed.), third ed., Society of Petroleum Engineers, Richardson, Texas, 1987.

[11] C.H. Whitson, M.R. Brule, Phase Behavior, Monograph 20, Henry, L. Doherty Series, Society of Petroleum Engineers, Richardson, Texas, (2000).

[12] L.N. Mohinder (Ed.), Piping Handbook, seventh, ed., McGraw-Hill, New York, 1999.

[13] L.F. Moody, Friction Factors for Pipe Flow, Trans, ASME vol. 66 (1944) 671–678.

[14] B.E. Larock, R.W. Jeppson, G.Z.Watters, Hydraulics of Pipeline Systems, CRC Press, Boca Raton, Florida, 1999.

[15] Crane Company, Flow of Fluids through Valves, Fittings and Pipe, Technical Paper No. 410, 25th printing, (1991).

[16] J.P. Brill, H. Mukherjee, Multiphase Flow in Wells, Monograph vol. 17(1999), L. Henry, Doherty Series, Society of Petroleum Engineers, Richardson, Texas.

[17] H.D. Beggs, J.P. Brill, A Study of Two Phase Flow in Inclined Pipes,, Journal of Petroleum Technology vol. 25 (No. 5) (1973) 607–617.

[18] Y.M. Taitel, D. Barnea, A.E. Dukler, Modeling Flow Pattern Transitions for Steady Upward Gas-Liquid Flow in Vertical Tubes, AIChE Journal vol. 26 (1980) 245.

[19] PIPESIM Course, Information on Flow Correlations used within PIPESIM, (1997). 398 Y. Bai and Q. Bai

[20] H. Duns, N.C.J. Ros, Vertical Flow of Gas and Liquid Mixtures in Wells, Proc. 6th World Petroleum Congress, Section II, Paper 22-106, Frankfurt, 1963.

[21] J. Qrkifizewski, Predicting Two-Phase Pressure Drops in Vertical Pipes, Journal of Petroleum Technology (1967) 829–838.

[22] A.R. Hagedom, K.E. Brown, Experimental Study of Pressure Gradients Occurring During Continuous Two-Phase Flow in Small-Diameter Vertical Conduits, Journal of Petroleum Technology (1965) 475–484.

[23] H. Mukherjce, J.P. Brill, Liquid Holdup Correlations for Inclined Two-Phase Flow, Journal of Petroleum Technology (1983) 1003–1008.

[24] K.L. Aziz, G.W. Govier, M. Fogarasi, Pressure Drop in Wells Producing Oil and Gas, Journal of Canadian Petroleum Technology vol. 11 (1972) 38–48.

[25] K.H. Beniksen, D. Malnes, R. Moe, S. Nuland, The Dynamic Two-Fluid Model OLGA: Theory and Application, SPE Production Engineering 6 (1991) 171–180. SPE 19451.

[26] A. Ansari, N.D. Sylvester, O. Shoham, J.P. Brill, A Comprehensive Mechanistic Model for Upward Two-Phase Flow in Wellbores, SPE 20630, SPE Annual Technical Conference, 1990.

[27] A.C. Baker, K. Nielsen, A. Gabb, Pressure Loss, Liquid-holdup Calculations Developed, Oil & Gas Journal vol. 86 (No 11) (1988) 55–59.

[28] O. Flanigan, Effect of Uphill Flow on Pressure Drop in Design of Two-Phase Gathering Systems, Oil & Gas Journal vol. 56 (1958) 132–141.

[29] E.A. Dukler, et al., Gas-Liquid Flow in Pipelines, I. Research Results, AGA-API Project NX-28 (1969).

[30] R.V.A. Oliemana, Two-Phase Flow in Gas-Transmission Pipeline, ASME paper 76- Pet-25, presented at Petroleum Division ASME Meeting, Mexico City, (1976).

[31] W.G. Gray, Vertical Flow Correlation Gas Wells API Manual 14BM (1978).

[32] J.J. Xiao, O. Shoham, J.P. Brill, A Comprehensive Mechanistic Model for Two-Phase Flow in Pipelines, SPE, (1990). SPE 20631.

[33] S.F. Fayed, L. Otten, Comparing Measured with Calculated Multiphase Flow Pressure Drop, Oil & Gas Journal vol. 6 (1983) 136–144.

[34] Feesa Ltd, Hydrodynamic Slug Size in Multiphase Flowlines, retrieved from http:// www. feesa.net/flowassurance.(2003).

[35] Scandpower, OLGA 2000, OLGA School, Level I, II.

[36] Deepstar, Flow Assurance Design Guideline, Deepstar IV Project, DSIV CTR 4203b–1, (2001).

[37] J.C. Wu, Benefits of Dynamic Simulation of Piping and Pipelines, Paragon Technotes (2001).

[38] G.A. Gregory, Erosional Velocity Limitations for Oil and Gas Wells, Technical Note No. 5, Neotechnology Consultants Ltd, Calgary, Canada, 1991.

[39] American Petroleum Institute, Recommended Practice for Design and Installation of Offshore Platform Piping System, fifth edition,, API RP 14E, 1991.

[40] M.M. Salama, E.S. Venkatesh, Evaluation of API RP 14E Erosional Velocity Limitations for Offshore Gas Wells, OTC 4485 (1983). Hydraulics 399