A new adaptation of a proven flow simulator is aiding blowout contingency planning. Most important wells require a blowout contingency plan. Part of that plan includes relief well intervention. The flow simulator distinguishes between workable and difficult intervention schemes. It suggests any needed modifications in original well design. And it makes crisis management quicker, cheaper, and more effective. This paper describes the power of using this simulator for both surface and relief well hydraulic kill planning. Introduction Planning kill strategy for a 1989 underground blowout in the North Sea required development of an improved flow simulator. The hydraulic kill simulator was based on the industry-standard, two-phase pipe flow model, OLGA. After the project, the planning team realized that they gained considerable advantage from using a transient two-phase flow simulator for comparing various kill scenarios. Since then, OLGA-WELL-KILL simulator has been used successfully for a number of intervention design plans. In the event of a major blowout, the speed at which rescue and intervention equipment and personnel are mobilized is critical for the preservation of life, property, and the environment. The first priorities of these emergency operations are personnel evacuations, oil spill containment, and salvage of the reservoir, platform and well. To respond quickly and efficiently to these emergencies, operators have devised and supported emergency response plans with the necessary resources and infrastructure to react immediately if required. Unfortunately, the only way to test the true effectiveness of a response strategy is during an actual emergency. Only after the events can one evaluate results and make modifications. It is this reasoning, in the aftermath of recent major blowouts in the North Sea, that operators and regulatory authorities are re-evaluating the status of emergency response plans under their jurisdiction. Their purpose is to assure that lessons learned from these events are documented and that all operators incorporate appropriate improvements into their emergency procedures. One component of this post evaluation process indicated that additional preparation for regaining control of a blowing well is justified. Even though the probability of a blowout is small, the consequences in safety, cost, and pollution could be catastrophic. For these reasons, "solving the problem" contingency plans are being added to the existing emergency response plans. This effort will eventually include surface, subsea, and relief well intervention. A primary objective of this contingency planning process is to evaluate the current level of technology and operational expertise available for a blowout intervention operation. Shortfalls can then be identified and appropriate action taken to reduce the deficiencies. One problem identified early in this evaluation was the difficulty in analyzing heavy mud hydraulic kills, in a two-phase blowout flow regime, with existing steadystate flow models. These models cannot easily evaluate the time transients of the kill process or deal with complicated multiphase flow regimes, flow paths and interaction with the reservoir. P. 311^
An important factor in the exploitation of the world's oil and gas resources is the mode of transportation away from the exploration and production facilities to regions where processing can be performed. Commonly, pipelines are employed providing annual transport capability for billions of dollars worth of crude oil, natural gas and associated products. This paper focuses on the offshore transportation of crude oil via inter-platform and platform-shore flowline systems, In particular, the study addresses the dynamics of riser-flowline configurations under conditions generated by the topsides rupture of one of the risers. The problem is of a complex dynamic multiphase nature, necessitating the use of a reliable mathematical tool. Here, the OLGA code was used to provide predictions of the transient phenomena occurring in the system. Field data relating to operating conditions and fluid properties were used throughout the simulations. The investigations focus on the system dynamics subsequent to a rupture with the aim of predicting the mass release from the flowline-riser system. Various factors are seen to contribute to the resulting predictions. These include the oil bubble point pressure, flowline topology as well as modelling assumptions. Introduction Over the past recent years, events within the petroleum industry have contributed to a substantial increase, among pipeline operators, in the awareness of safety and environment related issues. As a result of this, increased efforts are now being made to employ the latest technology in pipeline integrity monitoring techniques. Offshore production platform scenarios, in particular; provide for a higher order of complexity in aspects of safety and loss prevention. The Cullen Report[l] calls for measures to mitigate the effects of any accident that may occur, one of which relates to the minimisation of hydrocarbon inventory on the platform and in risers and pipelines and isolation of pipelines. This may be achieved by the installation of valves that shut off flow. These may include topside emergency shut down valves (ESD) as well as subsea valves, whether a non-return valve (NRV), or a subsea isolation valve (SSIV). The effect of installat ion of a SSIV in a gas transport flowline is clear in that the maximum inventory available for evacuation through a rupture is bounded by the SSIV. In the case of an oil line the hydrocarbon release may be said to be governed by a mobility effect determined by, among other factors, the oil volatility. The merits for installation of a SSIV in an oil line must therefore be investigated on a case by case basis. Such investigations necessitate an appreciation of the phenomena associated with the dynamics of pipelines under leaking or rupture conditions. This paper shall address the latter topic, reporting the application of the OLGA model to the rupture of crude oil lines. A brief approach to pipeline rupture calculations will first be presented followed by a description of OLGA. The application of the model to cases of riser rupture is presented next with model predictions subsequently detailed and discussed.
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