The objective of this study is to describe the complete transport chain of CO2 between capture and storage including a ship transport. This last one is composed by the following steps: Shore terminal including the liquefaction, temporary storage and CO2 loading, Ship with a capacity of 30,000 m 3 , On or off shore terminal including an unloading system, temporary storage and export towards the final storage. Between all the possible thermodynamic states, the liquid one is most relevant two options are compared in the study (-50°C, 7 bar) and (-30°C, 15 bar). The ship has an autonomy of 6 days, is able to cover 1,000 km with a cargo of 2.5 Mt/year. Several scenarios are studied varying the geographical position of the CO2 source, the number of harbours and the way the CO2 is finally stored. Depending on the option, the transport cost varies from 24 to 32 €/tCO2. This study confirms the conclusion of a previous study supported by ADEME, the cost transport is not negligible regarding the capture one when ships are considered. Transport by ship becomes a more economical option compared with an off shore pipeline when the distance exceeds 350 km and with an onshore pipeline when it exceeds 1,100 km .

Homogenous oil in water dispersion has been investigated in a horizontal pipe. The mean droplet size is 25 lm. Experiments were carried out in a 7.5-m-long transparent pipe of 50-mm internal diameter. The wall friction has been measured and modeled for a wide range of flow parameters, mixture velocities ranging from 0.28 to 1.2 m/s, and dispersed phase volume fractions up to 0.6, including turbulent, intermediate, and laminar regimes. Flow regimes have been identified from velocity profiles measured by particle image velocimetry in a matched refractive index medium. It is shown that the concept of effective viscosity is relevant to scale the friction at the wall of the dispersed flow. Based on mixture properties, the friction factor follows the Hagen-Poiseuille and the Blasius' law in laminar and turbulent regimes, respectively. Interestingly, the transition toward turbulence is delayed as the dispersed phase fraction is increased.

An experimental study is presented of a liquid–liquid dispersed/stratified flow in a horizontal pipe. The flow studied contains a highly concentrated layer of oil drops (light phase) under which flows a continuous layer of aqueous phase (heavy phase). The instant flow structure and hydrodynamics have been characterized in the aqueous phase using Particle Image Velocimetry in a matched refractive index medium. In this article, we focus on momentum transfer in the continuous aqueous layer at the wall, and at the interface, between the aqueous layer and the concentrated layer of oil drops. It is shown that, despite the presence of secondary flows, the velocity profile in the aqueous phase follows the classical logarithmic law near the wall. The shape of the tangential Reynolds stress profile in the aqueous layer is discussed in relation with the flow geometry and the presence of secondary flows. The mean interfacial shear stress is then derived from the macroscopic momentum balance applied in the aqueous layer cross‐section. The local viscous stress contribution below the interface has been identified from the momentum balance equation in the vertical direction and an effective viscosity as a function of the local concentration has been derived. © 2007 American Institute of Chemical Engineers AIChE J, 2007

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