Server maintenance is scheduled for Saturday, December 21st between 6am-10am CST.
During that time, parts of our website will be affected until maintenance is completed. Thank you for your patience.
Use GIVING24 at checkout to save 20% on eCourses and books (some exclusions apply)!
The paper discusses how SRFeCO3 affects the stability of the corrosion product films and how SRFeCO3 can be used to estimate the equilibrium pressure of H2S in the annulus.
We are unable to complete this action. Please try again at a later time.
If this error continues to occur, please contact AMPP Customer Support for assistance.
Error Message:
Please login to use Standards Credits*
* AMPP Members receive Standards Credits in order to redeem eligible Standards and Reports in the Store
You are not a Member.
AMPP Members enjoy many benefits, including Standards Credits which can be used to redeem eligible Standards and Reports in the Store.
You can visit the Membership Page to learn about the benefits of membership.
You have previously purchased this item.
Go to Downloadable Products in your AMPP Store profile to find this item.
You do not have sufficient Standards Credits to claim this item.
Click on 'ADD TO CART' to purchase this item.
Your Standards Credit(s)
1
Remaining Credits
0
Please review your transaction.
Click on 'REDEEM' to use your Standards Credits to claim this item.
You have successfully redeemed:
Go to Downloadable Products in your AMPP Store Profile to find and download this item.
Slurry pipeline systems are used for the extraction of bitumen from mined ore in the oil sands industry in Alberta, Canada. Most of these extraction processes are open to atmosphere resulting in significant air ingress and entrainment within the slurry pipelines used to transport mined ore and tailings. In addition, for short hydrotransport slurry pipelines, the slurry is conditioned by air to create bubbles coated with a bitumen film called “air-sacks”.
The efforts to lower automotive component weight to make cars more fuel efficient has increased the demand for aluminum alloys. In these applications, substantial amounts of heat are generated due to engine combustion, making it necessary to cool the engine systems. Metals in an engine application will rely on coolant to transfer heat. Corrosion behavior is another consideration for metals. Aluminum alloys, similar to the metals they are replacing, are sensitive to corrosion, especially in an aqueous alkaline environment.
A suitable acid package in matrix acidizing application is very important to the stimulation employed to improve the productivity of carbonate reservoirs. Typically, concentrated acids between 5 and 28 wt% are used and the most used mineral acid for carbonate acidizing treatment is hydrochloric acid (HCl) 1,2. A significant challenge of acidizing treatment is corrosion loss of metal tubulars due to the high reactivity of acid and metal, especially at high temperatures. Corrosion inhibitors are needed to reduce the corrosion loss of steel surface of facilities exposed in acidic environment.
Corrosion of pipelines made of carbon steel and exposed to wet hydrocarbons containing CO2 and H2S is a common but serious problem encountered in petroleum industry and its occurrence causes enormousexpense due to production downtime, accidental injuries, and replacement costs. Control and prevent corrosion using chemical treatment (e.g. corrosion inhibitor injection) is one of the most cost-effective solutions and commonly practiced methods to prevent corrosion failures in pipelines in oil and gas industry. Generally speaking, the active corrosion inhibitor (CI) components in commercial CI packages are usually organic, nitrogen-based surfactants such as amines, imidazoline and its derivatives. Due to the amphiphilic nature of surfactants, a good fraction of the injected CI will inevitably go into the oil phase through partitioning and to the oil/water interface.
Corrosion inhibitors provide a critical barrier to internal corrosion, presenting the most cost-effective form of mitigation and enabling operators to use carbon steel where it would otherwise be impractical. The correct selection and validation of inhibitors is essential to ensure successful field deployment, providing safe and reliable operation. However, the selection and optimization of a corrosion inhibitor for a particular field application is not trivial.
In the first paper, a mixture design matrix of a homologous series of alkyldimethylbenzylammonium chlorides (BAC) was used to assess the performance and facilitate optimization of a mixed surfactant corrosion inhibitor system based on surface coverage and steady state inhibited corrosion rate.1 In this second paper, the approach is extended to include adsorption kinetic analysis, as demonstrated in Woollam and Betancourt for a first-order Langmuir kinetic model.2
Corrosion continues to be a threat to the petroleum industry. It risks people’s lives, the environment, and assets integrity, in addition to the financial losses. In fact, the annual global cost of corrosion was estimated in 2013 to be around US$2.5 trillion (3.2% of 2013 global GDP). Of this amount, approximately 15-35% (i.e. US$375 to US$875 billion annually) can be avoided through proper corrosion control management and advanced mitigation technologies
Carbon steel (CS) material is widely used for the equipment in oil and gas production industry due to its mechanical properties associated with a relatively low cost, compared to other materials. Depending on the corrosiveness of the fluid that is vehiculated, the use of carbon steel is generally associated with the injection of a corrosion inhibitor (CI) in order to mitigate internal corrosion. Corrosion inhibitors are generally used in continuous injection at an injection rate that is depending on the corrosiveness of the fluid. Based on the operational feedback, the internal standards are recommending for multiphase pipelines CI injection rates in the range of 50 - 70 ppm for temperature below 80°C of and of 150 to 200ppm for temperatures above 100°C. These injection dosages are typical values that are considered in the laboratory tests for the qualification of the CI and they are adjusted on-site based on the monitoring results.
M. B. Kermani pointed out that 25% of equipment failures in the oil and gas industry are caused by corrosion, and more than half of corrosion events are related to produced fluids containing CO2 and H2S. In recent years, the exploitation of sour oil and gas fields (containing H2S or H2S/CO2 mixture) has become more and more common, and prominent problems such as tubing ruptures caused by pitting and uniform corrosion have appeared. In oil fields containing CO2 and H2S, local corrosion is a key factor restricting the selection of tubing and casing materials. In an oilfield containing CO2 and H2S in the Middle East, the authors corroded coupons on site, and carried out indoor simulation experiments for the problems found in the field test. The authors systematically studied 13Cr, S13Cr, 22Cr, 25Cr and 2550 in the presence of H2S, CO2 and high mineralization.
The unstable oil market demand in the petroleum industry, the oil financial crisis and the Covid-19 pandemic have pushed the Oil and Gas operators to look for optimized, cost effective and more reliable strategies of design and operation. Large part of CAPEX is invested in the well materials. Hence, materials of Oil and Gas wells should be selected to withstand both internal and external threats to ensure integrity and availability while maintaining on focus on affordability over the lifecycle.1
The terminal is subdivided for Oil, Gas and Produced Water plants. Each of these plants has number of storage tanks. The age of the tanks varies between 15-25 years. The products held within these tanks varies, from crude oil, condensate, produced water, potable water, to off spec oil and diesel fuel.
Most of the tanks within the facility have a similar CP arrangement and design. Each tank base is protected by an impressed current grid mesh anode buried in compacted, clean, sand backfill beneath the tank base and is powered by a transformer-rectifier placed outside the bund wall or within an electrical switch room. Permanent reference electrodes are installed beneath all tank bases to enable accurate potential measurements. Reference electrodes vary from Copper/Copper Sulphate, Silver/Silver Chloride to Zinc.