Dew Points of Ternary Methane (or Ethane) + Carbon Dioxide + Water Mixtures: Measurement and Correlation (original) (raw)
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Industrial & Engineering Chemistry Research, 2006
Dew points have been measured for binary propane or n-butane + carbon dioxide mixtures at pressures from 1.2 × 10 5 to 34.9 × 10 5 Pa and temperatures from 192.6 to 274.8 K, four ternary propane or n-butane + carbon dioxide + water mixtures from 1.1 × 10 5 to 20.7 × 10 5 Pa and temperatures from 247.5 to 289.0 K, and eight quaternary propane or n-butane + carbon dioxide + water + methanol mixtures from 1.1 × 10 5 to 21.8 × 10 5 Pa and temperatures from 249.8 to 289.9 K. The results are analyzed in terms of a predictive EF-EOS excess-function equation of state method based on the zeroth-approximation of Guggenheim's reticular model. This method has been chosen because it can be used to adequately predict the dew points of all the mixtures of our interest in the dew temperature and pressure ranges. In fact, the model reproduces the experimental dew-point temperature data within an AAD (absolute average deviation) of 1.6 and 1.3 K for the binary systems, between 0.1 and 2.5 K for the ternary systems, and between 0.0 and 5.1 K for the quaternary systems. The experimental results obtained for ternary propane or n-butane + carbon dioxide + water mixtures at pressure values higher than 5 × 10 5 Pa were also compared to a predictive EOS (equation of state) model. It reproduced experimental dew-point temperature data within AAD between 0.0 and 5.5 K.
Dew points of binary carbon dioxide + water and ternary carbon dioxide + water + methanol mixtures
Fluid Phase Equilibria, 2004
Dew points for four carbon dioxide + water mixtures between 1.2 × 10 5 and 41.1 × 10 5 Pa in the temperature range from 251.9 to 288.2 K, and eight carbon dioxide + water + methanol mixtures between 1.2 × 10 5 and 43.5 × 10 5 Pa and temperatures from 246.0 to 289.0 K were experimentally determined. The experimental results obtained on the binary and ternary systems were analysed in terms of a predictive excess function-equation of state (EF-EOS) method, which reproduced the experimental dew point temperature data with absolute average deviation (AAD) between 0.8 and 1.8 K for the systems with water, and from 0.0 to 2.7 K for the systems with water and methanol. The experimental results obtained for carbon dioxide + water mixtures, with molar fraction of water lower than 0.00174, at pressure values higher than 5 × 10 5 Pa were also compared to a predictive equation of state model. It reproduced experimental dew point temperature data with AAD between 0.2 and 0.6 K.
Measurement and prediction of dew point curves of natural gas mixtures
Fluid Phase Equilibria, 2012
Dew point measurements for six synthetic natural gas (SNG) mixtures were performed using a custom made chilled mirror apparatus. The experimental data cover a temperature-range from 253 to 285 K and a pressure-range from 3 to 105 bar. The recently developed UMR-PRU model was revised and applied to these experimental data as well as to other dew point data for synthetic and two real natural gas mixtures reported in the literature. The results of the UMR-PRU model were compared to those obtained by the Peng-Robinson equation of state coupled with the classical van der Waals one fluid mixing rules using either zero interaction parameters or temperature dependent ones utilized in a predictive version of the PR EoS, the so-called PPR78 EoS.
Energy & Fuels, 2003
Dew points for two synthetic natural gas (SNG) mixtures between 1.2 × 10 5 and 81.8 × 10 5 Pa in the temperature range from 213.6 to 261.4 K, four SNG + water mixtures between 1.1 × 10 5 and 41.0 × 10 5 Pa and temperatures from 244.7 to 288.1 K, and four SNG + water + methanol mixtures between 1.1 × 10 5 and 20.7 × 10 5 Pa and temperatures from 247.6 to 288.6 K were experimentally determined. The experimental results obtained on the multicomponent systems were analyzed in terms of a predictive excess function-equation of state (EF-EOS) method, which reproduced experimental dew point temperature data with absolute average deviation (AAD) between 0.9 and 3.1 K for the dry systems, from 0.0 to 1.6 K for the systems with water, and from 0.0 to 3.0 K for the systems with water and methanol. The experimental results obtained for synthetic natural gas (SNG) + water mixtures at pressure values higher than 5 × 10 5 Pa were also compared to a predictive equation of state (EOS) model. It reproduced experimental dew point temperature data within AAD between 1.8 and 5.3 K.
Energy & Fuels, 2002
Dew points for two synthetic natural gas (SNG) mixtures between 1.2 × 10 5 and 81.8 × 10 5 Pa in the temperature range from 213.6 to 261.4 K, four SNG + water mixtures between 1.1 × 10 5 and 41.0 × 10 5 Pa and temperatures from 244.7 to 288.1 K, and four SNG + water + methanol mixtures between 1.1 × 10 5 and 20.7 × 10 5 Pa and temperatures from 247.6 to 288.6 K were experimentally determined. The experimental results obtained on the multicomponent systems were analyzed in terms of a predictive excess function-equation of state (EF-EOS) method, which reproduced experimental dew point temperature data with absolute average deviation (AAD) between 0.9 and 3.1 K for the dry systems, from 0.0 to 1.6 K for the systems with water, and from 0.0 to 3.0 K for the systems with water and methanol. The experimental results obtained for synthetic natural gas (SNG) + water mixtures at pressure values higher than 5 × 10 5 Pa were also compared to a predictive equation of state (EOS) model. It reproduced experimental dew point temperature data within AAD between 1.8 and 5.3 K.
A New Correlation to Predict Dew Point Pressure in Wet Gas Reservoirs
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Water is probably the most undesirable component found in crude natural gas because its presence can produce hydrate formation, and it can also lead to corrosion or erosion problems in pipes and equipment. Natural gas must be dehydrated before being transported through a long distance to ensure an efficient and trouble-free operation. Thermodynamic modelling of triethyleneglycol (TEG)-water system is still rather inaccurate, especially with regard to systems at high temperature and high TEG concentration. As a consequence, design and operation of absorber towers are affected by the lack of accurate data. Two novel correlations have been developed to estimate the equilibrium water dew point of a natural gas stream by evaluating experimental data and literature. These data were collected and analyzed by means of images scanned with MATLAB software R2012B version. An average percentage error is of 1-2% for linear correlation and it is of 2-3% for non-linear correlation. Results are quite accurate and they are consistent with literature data. Due to the simplicity and precision of the correlations developed in this work, the equations obtained have a great practical value. Consequently, they allow process engineers to perform a quick check of the water dew point at different conditions without using complex expressions or graphics.
Toward a predictive model for estimating dew point pressure in gas condensate systems
Fuel Processing Technology, 2013
Dew-point pressure is one of the most important quantities for characterizing and successful prediction of the future performance of gas condensate reservoirs. The objective of this study is to present a reliable, computerbased predictive model for prediction of dew-point pressure in gas condensate reservoirs. An intelligent approach based on least square support vector machine (LSSVM) modeling was developed for this purpose. To this end, the model was developed and tested using a total set of 562 experimental data points from different retrograde gas condensate fluids covering a wide range of variables. Coupled simulated annealing (CSA) was employed for optimization of hyper-parameters of the model. The results showed that the developed model significantly outperforms all the existing methods and provide predictions in acceptable agreement with experimental data. In addition, it is shown that the proposed model is capable of simulating the actual physical trend of the dew-point pressure versus temperature for a constant composition fluid on the phase envelope.
A new Peng-Robinson modification to enhance dew point estimations of natural gases
Journal of Natural Gas Science and Engineering, 2016
Equations of state (EOSs) are widely used in calculations such as those involving reservoir simulation, process simulation, gas processing and transportation of natural gas. Predicting the phase envelope, specifically the dew points of natural gas, is among the important roles of EOSs. In this study, a modification is proposed to improve the predictions of dew point properties by the Peng-Robinson (PR) EOS, where the attraction parameter has been modified by a new empirical-based coefficient which is a function of reduced pressure, reduced temperature and critical density. In order to validate the modification, results are presented for four major properties of dew points consisting of the cricondentherm, cricondenbar, dew point temperature and dew point pressure. Furthermore, the performances of the original PR, Soave-Redlich-Kwong (SRK), Schmidt-Wenzel (SW) and GERG-2008 EOSs, have been compared to predict the above four properties with respect to the experimental data. Having similar qualitative trends for the four properties, the results show that the modification of this study gives better predictions of the dew point curves, followed by the GERG EOS, which was developed particularly for processed natural gases. The SRK and SW EOSs have comparatively similar results and the PR EOS has the largest deviations.
Effect of Dew Point Depression on Molecular Weight Determination of Hydrocarbon Mixture
The molecular weight of components of four hydrocarbon mixtures n-Nonane+n-Tetradecane, n-Hexane+n-Nonane, n-Hexane+Toluene, and Toluene+n-Tetradecane were determined by an experimental procedure based on freezing point depression. The results showed a marked improvement from the values obtained using the Kay’s mixing rule, for the molecular weight determination of multicomponent mixtures. The results also form the bases for the determination of the critical properties of hydrocarbon mixtures.