Substitution of Carbon Steels for ASME SA-533 Type E for Lightweight Equipment

International audienceThe use of MnMo(Ni) alloys ASME SA-533 type B or type C in lieu of carbon manganese steels (SA-516 Grade 65 or Grade 70) started about 30 years ago to produce lightweight pressure vessels. But the development of these low alloy steels for the fabrication of equipment for wet H2S service ("sour service") remains limited due to their weldability considered as challenging. This paper aims at introducing newly developed material ASME SA-533 type E class 2, and provides results obtained in base metal and welded joints, especially with respect to NACE standard MR0175 / ISO 15156-2. Finally, a case study on an absorber for amine gas treating units (AGRU) will be described to illustrate the mass savings that can be achieved with SA-533 type E class 2

Isothermal phase (vapour + liquid) equilibrium data for binary mixturesof propene (R1270) with either 1,1,2,3,3,3-hexafluoro-1-propene(R1216) or 2,2,3-trifluoro-3-(trifluoromethyl)oxirane in the temperature range of (279 to 318) K range.

International audienceIsothermal (vapour + liquid) equilibrium data (P–x–y) are presented for the 1-propene +1,1,2,3,3,3-hexafluoro-1-propene and the 1-propene + 2,2,3-trifluoro-3-(trifluoromethyl)oxirane binary systems. Both binary systems were studied at five temperatures, ranging from (279.36 to 318.09) K, atpressures up to 2 MPa. The experimental (vapour + liquid) equilibrium data were measured using an apparatus based on the ‘‘(static + analytic)’’ method incorporating a single movable Rapid On-Line Sampler-Injector to sample the liquid and vapour phases at equilibrium. The expanded uncertainties are approximated on average as = 0.07 K, 0.008 MPa, and 0.007 and 0.009 for the temperature, pressure, and the liquid and vapour mole fractions, respectively. A homogenous maximum-pressure azeotrope was observed for both binary systems at all temperatures studied. The experimental data were correlated with the Peng–Robinson equation of state using the Mathias–Copeman alpha function, paired with theWong–Sandler mixing rule and the Non-Random Two Liquid activity coefficient model. The model provided satisfactory representation of the phase equilibrium data measure

Alternative metallurgies reduce the cost of amine gas treating units

International audienceProduction facilities, including platforms or FPSO, are becoming more and more complex structures. Reducing the weight of the process units is an important challenge, and represents a huge source of costs savings. IFPEN, PROSERNAT and INDUSTEEL have evaluated two alternative metallurgies with high mechanical properties to reduce the weight of equipment of amine gas treating units (AGRU). Duplex stainless steels are considered as an alternative to more conventional austenitic stainless steel grades. High strength alloy steel ASME SA-533 type E class 2, having an UTS above 90 ksi, can be an alternate to carbon steel ASME SA-516 Gr65 type (UTS 65 ksi). The compatibility of these steel grades with amine service was checked through autoclave corrosion tests in amine solutions. Various experiments were performed in conditions representative of the bottom part of absorber and of upper section of regenerator of AGRU, with variable loadings of CO 2 and H 2 S. Study used different specimens: weight-loss coupons, four-point-bend assemblies, and U-bends. For all these tests, alternative metallurgies proved to behave at least as well as the reference ones generally considered in amine plants with no significant corrosion nor cracking. In addition to experimental tests and presentation of steel properties, the paper describes a case study of AGRU where the mass gain and CAPEX benefits are elaborated for a 75 bar, 4.5 meters diameter absorber, and for a 4.8 meters diameter, low pressure, stripper

Isothermal vapor-liquid equilibrium data for the 1,1,2,2-tetrafluoroethene + 1,1,2,3,3,3-hexafluoroprop-1-ene binary system : measurement and modeling from (248 to 283) K

Isothermal vapor−liquid equilibrium data are presented for the 1,1,2,2-tetrafluoroethylene and 1,1,2,3,3,3-hexafluoroprop-1-ene binary system at (248.14, 263.01, and 282.89) K, with pressures ranging from (0.12 to 2.35) MPa. An apparatus based on the “static−analytic” method, equipped with a movable rapid online sampler−injector (ROLSI), was used to undertake the measurements. The combined expanded uncertainties are estimated at 0.11 K, 4 kPa, and 0.012 and 0.009 for the temperature, pressure, and the equilibrium liquid and vapor mole fractions, respectively. The experimental data were correlated with the Peng−Robinson equation of state using the Mathias −Copeman α function, together with the Wong−Sandler mixing rule utilizing the nonrandom two-liquid activity coefficient model.National Research Foundation of South Africa under the South African Research Chair Initiative of the Department of Science and Technology.http://pubs.acs.org/loi/jceaaxhb201

Isothermal vapor-liquid equilibrium data for the 1,1,2,3,3,3-hexafluoroprop-1-ene +1,1,2,2,3,3,4,4-octafluorocyclobutane binary system : measurement and modeling from (292 to 352) K and pressures up to 2.6 Mpa

Isothermal vapor–liquid equilibrium data are presented for the 1,1,2,2-tetrafluoroethylene and 1,1,2,3,3,3-hexafluoroprop-1-ene binary system at (248.14, 263.01, and 282.89) K, with pressures ranging from (0.12 to 2.35) MPa. An apparatus based on the “static–analytic” method, equipped with a movable rapid online sampler–injector (ROLSI), was used to undertake the measurements. The combined expanded uncertainties are estimated at 0.11 K, 4 kPa, and 0.012 and 0.009 for the temperature, pressure, and the equilibrium liquid and vapor mole fractions, respectively. The experimental data were correlated with the Peng–Robinson equation of state using the Mathias–Copeman α function, together with the Wong–Sandler mixing rule utilizing the nonrandom two-liquid activity coefficient model.National Research Foundation of South Africa under the South African Research Chair Initiative of the Department of Science and Technology.http://pubs.acs.org/loi/jceaax2016-03-31hb201

Détermination de coefficients de partage et de limites de solubilité du méthanol dans des mélanges liquides comportant azote et hydrocarbure(s) aux conditions opératoires des unités de fractionnement du gaz naturel

After natural gas treatment, methanol is found as a trace contaminant. Our objective is to determine thermodynamic properties of “hydrocarbon(s) – methanol” mixtures at operating conditions related to fractionators, at high and low temperatures. In effect, industries may be penalized financially when methanol composition is higher than 50 ppm moles in final products. Therefore, our aim is to understand phase equilibrium at specific conditions of these units. There is almost no literature for such little methanol quantities. Furthermore, thermodynamic models (predictive and with parameters adjusted for the whole composition range) do not allow correct representation of “vapor – liquid” equilibrium at infinite dilution. A “static – analytic” still with phase sampling and GC analysis is used to perform these measurements. At high temperatures, we have determined methanol partition coefficients. The equipment has been adapted, along time, to increase methanol trace quantifications (molar fractions below 1 000 ppm). A unique calibration procedure taking into account methanol adsorption during the analysis stage was developed. New measurements show that for the studied composition range and within the experimental uncertainty, total pressures of the system and methanol partition coefficients are only temperature dependant. The methanol Henry's law constants as well as infinite dilution activity coefficients in the different hydrocarbon mixtures are calculated. At low temperatures, we are interested in determining the methanol limiting solubilities in “nitrogen – hydrocarbon(s)” liquid mixtures. An apparatus is under development to realize these measurements. Our new specific measurements will be used as a basis for fractionator process simulators, to estimate as precisely as possible methanol contents inside fractionator products.Après le traitement du gaz naturel, le méthanol est présent sous forme de traces. Notre objectif est de déterminer les propriétés thermodynamiques des mélanges “hydrocarbure(s) – méthanol“ aux conditions opératoires rencontrées lors du fractionnement du gaz naturel, à hautes et basses températures. En effet, les industries peuvent être pénalisées financièrement lorsque la teneur finale en méthanol dépasse 50 ppm molaire. Pour cela, nous souhaitons connaître les équilibres entre phases aux conditions spécifiques régnant dans ces unités. Peu de données existent pour de si faibles teneurs en méthanol. De plus, les modèles thermodynamiques utilisables sur l'ensemble du domaine de compositions ne permettent pas de représenter correctement les équilibres à dilution infinie. Un appareillage, basé sur une technique "statique-analytique" avec échantillonnages des phases et analyse par CPG est utilisé. A hautes températures, nous avons déterminé les coefficients de partage du méthanol. L'appareillage a été adapté au cours du temps, afin d'améliorer la quantification de traces de méthanol (inférieures à 1 000 ppm). Une procédure d'étalonnage originale tenant compte de l'adsorption du méthanol dans les circuits d'analyse a été mise au point. Les nouvelles mesures montrent qu'à l'incertitude expérimentale près, la pression totale du système ainsi que le coefficient de partage du méthanol sont seulement fonctions de la température. Les constantes de la loi de Henry ainsi que les coefficients d'activité à dilution infinie du méthanol sont calculés. A basses températures, nous souhaitons déterminer les valeurs limites de solubilité du méthanol dans les mélanges liquides : azote - hydrocarbure(s). Un appareillage est en cours d'adaptation pour réaliser ces mesures. Les nouvelles données serviront de bases au développement des simulateurs de procédés de fractionnement, en vue d'estimer le plus précisément possible les teneurs en méthanol dans les hydrocarbures produits

Détermination de coefficients de partage et de limites de solubilité du méthanol dans des mélanges liquides comportant azote et hydrocarbure(s) aux conditions opératoires des unités de fractionnement du gaz naturel

PARIS-MINES ParisTech (751062310) / SudocSudocFranceF

Etude de la distribution du méthanol dans le cadre de procédés de fractionnement des composés du gaz naturel

International audienc

Methanol distribution in natural gas fractionators

International audienc

Hydraulic and mass transfer performances of a commercial hybrid packing: the RSP200X -Key modelling parameters for gas treatment applications

International audienceThe RSP200X , as one of the latest generation of Raschig's structured packings (Raschig Super-Pak ,RSP), has been investigated for use in scrubbing columns operating at high liquid loads where it could be particularly well adapted. These RSP packings offer a good potential for increasing capacity while maintaining mass transfer efficiencies at high levels. IFPEN has measured hydraulic and mass transfer performances in two columns of different diameters (146 mm and 1000 mm). Flooding limits were in agreement with literature, however at high liquid loads and for the tested X-Style RSP they were 30-40% lower than those calculated with the Winsorp Software delivered by Raschig. With the support of the present results a modified version of Winsorp has been elaborated for high liquid loads and X-Style RSP. In terms of mass transfer, the CO 2 /MDEA system was used to measure k L a e while the classic CO2/NaOH and SO2/NaOH systems were used for ae and kGae measurements. The RSP200X was found to develop a high interfacial area compared to its geometric area. While for standard packings the gas flow rate is often considered to have only a small effect on effective area when operating below the loading point, its effect measured on RSP200X is significant and of the same order as for liquid load. Measurements of k L a and k G a further confirm these trends