An amine plant campaign has been performed at the CO 2 Technology Centre Mongstad applying the aqueous 30 wt% and 40 wt% monoethanolamine (MEA) solvent systems for treatment of flue gas from a combined heat and power (CHP) plant. CHP flue gas flow rates were ranging from about 40.000 Sm 3 /h to 60.000 Sm 3 /h and the CO 2 content was about 3.5 vol%.Minimum specific reboiler duties (SRD) of respectively 4.0 MJ/kg CO 2 and 3.7 MJ/kg CO 2 were obtained for the aqueous 30 wt% MEA solvent system without and with the addition of anti-foam solution. A minimum SRD of 3.4 MJ/kg CO 2 was obtained for the aqueous 40 wt% MEA solvent system. Lower SRD and absorber liquid to gas (L/G) ratios were obtained with higher concentration MEA solvents.Increased absorber packing heights resulted in lower SRD. Variation in flue gas supply flow rates and corresponding variations in solvent flow rates, i.e. constant L/G ratios, did not yield any significant variations in SRD. Decreased flue gas supply temperatures resulted in lower SRD.For any future large scale post-combustion capture (PCC) amine plant, engineering aspects such as the flue gas supply temperature and instrumentation monitoring CO 2 content in the flue gas must be evaluated to avoid the chemical equilibrium pinch behavior. Engineering and environmental aspects related to the use of anti-foam solutions for future large scale PCC amine plants must also be considered.

Experimental pure component vapor pressure data for hexafluoropropylene (R1216) and hexafluoropropylene oxide (HFPO) are presented. Experimental vapor-liquid equilibrium (VLE) data are presented at two temperatures, (273 and 313) K, for four binary systems: R1216 + toluene, HFPO + toluene, hexafluoroethane (R116) + R1216, and R116 + HFPO. The measurements were undertaken using both a "static-analytic" apparatus fitted with a pneumatic rapid online sampler injector (ROLSI) and a "static-synthetic" PVT apparatus. The experimental vapor pressure data were regressed to obtain correlated parameters for the Peng-Robinson (PR) and Soave-Redlich-Kwong (SRK) equations of state with the Mathias-Copeman R function. The binary VLE data were regressed to obtain correlated parameters for three different model combinations: the PR equation of state with the Wong-Sandler (WS) mixing rules, the PR equation of state with the modified Huron-Vidal first-order (MHV1) mixing rules, and the SRK equation of state with the WS mixing rules. The Mathias-Copeman R function and the nonrandom two-liquid (NRTL) excess Gibbs energy model were used in conjunction with the equations of state and mixing rules. In general, the PR equation of state with the WS mixing rules provided the best correlation for the experimental data. The critical lines for the supercritical systems R116 + R1216 and R116 + HFPO, calculated with the PR equation of state with the WS mixing rules, are also presented.

Isothermal vapor−liquid equilibrium data were measured for the binary system 1,1,2,3,3,3-hexafluoro-1-propene +2,2,3-trifluoro-3-(trifluoromethyl)-oxirane from (268 to 308) K using an apparatus based on the "static-analytic" method. The expanded uncertainties in the measurements were evaluated as 0.05 K, 0.6 kPa, 0.002, and 0.003 for the temperature, pressure, and liquid and vapor mole fractions, respectively. The experimental data were correlated with the Peng− Robinson equation of state using the classical mixing rule and the Mathias− Copeman alpha function. No azeotropes were observed within the temperature and pressure range studied; however, the binary mixture had relative volatilities close to unity, indicating that separation of the mixture via standard distillation is not feasible. a Volume fraction stated by the Nuclear Energy Corporation of South Africa. b Area percentage of component identified by gas chromatography using a thermal conductivity detector (TCD) and a 5% Krytox CarboBlack B column.Article pubs.acs.org/jced

Isothermal vapor−liquid equilibrium (VLE) data for the binary systems R-744 + HFP and R-744 + HFPO were measured at (273.15 and 313.15) K and pressures up to 5.6 MPa. Measurements were also undertaken for the HFP + R-123 and HFPO + R-123 systems at (313.15 and 333.15) K and pressures up to 1.5 MPa. The VLE data were measured via the “static-analytic” method using a fixed-volume equilibrium cell equipped with a pneumatic ROLSI sampler. The measured data have maximum uncertainties of 0.045 K and 0.003 MPa in temperature and pressure, respectively, while the relative uncertainties in the equilibrium phase analyses are within 1 % for the molar compositions. The experimental data were correlated using the Peng−Robinson equation of state with the Mathias−Copeman α function and the Wong−Sandler mixing rules incorporating the NRTL activity coefficient model.