Équilibre vapeur-liquide
English
COMPARTILHAR
Visão Geral
Source : Michael G. Benton et Kerry M. Dooley, département de génie chimique, Louisiana State University, Baton Rouge, Louisiane
Équilibre de vapeur-liquide est primordiale dans les applications telles que la distillation, modélisation environnementale et la conception du processus général d’ingénierie. Comprendre les interactions entre les composants d’un mélange est très important dans la conception, d’exploitation et analyser ces séparateurs. Le coefficient d’activité est un excellent outil pour ce qui concerne les interactions moléculaires à la composition du mélange. Trouver les paramètres d’interaction moléculaire permet de prédire avenir des coefficients d’activité pour un mélange à l’aide d’un modèle.
Équilibre de vapeur-liquide est un facteur essentiel dans les processus communs dans l’industrie chimique, comme la distillation. La distillation est le processus de séparation des liquides par leur point d’ébullition. Un mélange liquide est introduit dans une unité de distillation ou de la colonne, puis bouilli. Données d’équilibre de vapeur-liquide sont utiles pour les mélanges liquides comment déterminants seront séparera. Parce que les liquides ont différents points d’ébullition, un liquide va bouillir en vapeur et progresser dans la colonne, alors que l’autre va rester sous forme liquide et égoutter dans l’unité. Le processus est très important dans une variété d’industries.
Dans cette expérience, les coefficients d’activité des mélanges de diverses compositions de méthanol, alcool isopropylique et d’eau déionisée seront obtenues à l’aide d’un dispositif d’équilibre de vapeur-liquide et le chromatographe en phase gazeuse. En outre, les paramètres d’interaction binaire du système seront déterminés en utilisant l’équation de Wilson et les coefficients d’activité.
Princípios
Équilibre de vapeur-liquide est un État où se trouve un composant pur ou un mélange de phases liquide et vapeur, avec un équilibre mécanique et thermique et aucun transfert de masse nette entre les deux phases. Liquide et vapeur sont séparées par la gravité et de la chaleur (Figure 1). Le mélange liquide est inséré dans le système, qui est mis dans un état vide avec une pompe à vide. La vapeur est condensée et retournée à mélanger avec du liquide, qui est ensuite transmis à la chambre de bouillante. Différences dans les résultats de point d’ébullition à une séparation du mélange. Le point d’ébullition de l’eau est plus élevé que celle des composants ajoutés, donc les composants volatils commencent à s’évaporer.
Figure 1 : Une représentation de l’appareil
Un coefficient d’activité est défini comme le rapport entre la fugacité d’un composant dans un mélange réel à la fugacité de la solution idéale de même composition. Fugacité est une propriété utilisée pour montrer les différences entre les potentiels chimiques à États standards. Vapor phase fugacités peuvent être exprimées en fonction d’un coefficient de fugacité [φ : fjeV = φ j’yj’ai fj’ai0V ], avec yj’ai = fraction molaire d’i dans la phase vapeur et fj’ai0V = la vapeur standard fugacité d’État (la fugacité de la vapeur de purs à T et P). Pour les faibles pressions, comme dans cette expérience, φj’ai = 1 et fj’ai0V = P. liquide fugacités de phase peuvent être exprimées en termes d’une activité coefficient γj’ai: fiL = γi xi fi 0 L , avec xj’ai = fraction molaire de i dans la phase liquide et fj’ai0 L = la fugacité de l’état liquide.
À la pression de saturation (Pis) de ce T, la fugacité de liquides purs est Pis, car la vapeur pure et le liquide sont en équilibre. Fugacités liquides étant uniquement des fonctions de pression faibles, nous pouvons rapprochant la fugacité liquides purs à T et P (fj’ai0 L) Pis, tant que la différence entre Pis et P n’est pas grande. Cette approximation est généralement appelée « négliger la correction de Poynting ». Si les expérimentateurs utilisent un appareil VLE pour mesurer la composition de la vapeur et le liquide qui est en équilibre, expérimentateurs peuvent calculer directement les coefficients d’activité fournis également mesurer P et T. T doit être mesuré pour déterminer PjeS pour tous j’ai.
Au cœur du dispositif VLE, utilisé dans cette expérience pour déterminer la composition des mélanges, est une pompe Cottrell qui « crache » le liquide bouillant dans une chambre bien isolée, de l’équilibre. Deux vannes de prélèvement opéré par magnétisme permettent de retrait des échantillons de liquide et condensation de vapeur. Un grand réservoir permet d’amortir les pulsations de pression dans le système comme les commutateurs de soupape de commande marche-arrêt et des fluctuations causées par la pompe Cottrell. Une fuite lente peut être utilisée pour créer un équilibre entre le taux de retrait de l’air et le taux d’entrée d’air pour maintenir une pression constante, si nécessaire.
Manière comparable à résoudre pour l’équilibre de vapeur-liquide consiste à utiliser une variété de modèles. Loi de Raoult, la Loi de Dalton et la Loi de Henry sont des modèles tout théoriques qui peuvent trouver les données de concentration d’équilibre de vapeur-liquide. Les trois modèles sont liées à la proportionnalité des pressions partielles, la pression totale et les fractions molaires des substances. Équation de Wilson s’est avérée pour être précis pour les liquides miscibles, tout en n’étant ne pas trop complexes. En outre, le modèle de Wilson intègre coefficients d’activité pour tenir compte de l’écart par rapport à des valeurs idéales.
Procedimento
Resultados
The activity coefficients of the data do not show significant deviations from a mean value for each component (Table 1). This is as expected because for intermediate component compositions there are not large variations. However, components near 1 have γ's near 1. Low composition components have high γ's. Components highest in concentration in a mixture which will have a reduced deviation, therefore it will be closer to ideal (γ = 1). Components with lower concentrations in a mixture will have higher deviations, so their γ's will be greater than 1.
Table 1: Results of each sampling of the experimental data.
The data were fit to Wilson model parameters and the coefficients were calculated (Table 2). A simple reduction in the sum of squared residuals between experimental and Wilson equation (1) activity coefficients was used. This was achieved using Excel's solver function. The parity plot shown relates the Wilson's Equation model activity coefficients to the experimentally found activity coefficients. The experimental activity coefficients were calculated and graphically compared to the calculated model coefficients.
Table 2: Results of fitting the data to the Wilson model parameters.
(1)
The parameter values found were the best fit (Table 3). Ideally the correlation is along the y=x line; however, a significant correlation resembling the ideal scenario was found (Figure 2). The activity coefficients of the data did not show significant deviations from a mean value for each component, as expected. A reduction in the sum of squared residuals between experimental and Wilson equation activity coefficients was used with Excel's solver function. The parity plot relates the Wilson's Equation model activity coefficients to the experimentally found activity coefficients.
Table 3: Model parameters with water (a), MeOH (b), and IPA (c). The experimental values are compared to expected values.
Figure 2: Depiction of the correlation between the experimental activity coefficients and the model activity coefficients.
Applications and Summary
This experiment demonstrated the equilibration of methanol – isopropanol – water vapor-liquid mixtures at a constant P = 700 mm Hg and how to measure temperature and composition and calculate activity coefficients. The activity coefficients of the data did not significantly deviate from a mean value for each component, as expected. A reduction in the sum of squared residuals between experimental and Wilson equation activity coefficients was used with Excel's solver function. The parity plot relates the Wilson's Equation model activity coefficients to the experimentally found activity coefficients.
In the petroleum industry, distillation is the primary process for separation of petroleum products. Many oil refineries use distillation for crude oil1. Light hydrocarbons are separated from heavier particles, separating based on boiling points1. Heavy materials like gas oils collect in the lower plates, while light materials like propane and butane rise up1. Hydrocarbons, such as gasoline, jet, and diesel fuels, are separated1. This process is often repeated many times to fully separate and refine the products1. Refineries run these processes at steady state, constantly creating new products at maximum capacity, so efficiency is key1. Chemical engineers working on these processes focus on optimizing the efficiency of the production1.
Tray distillation columns are also used to separate a variety of chemical products. Ethanol is one such product. Through closely related processes, a variety of products such as fuel-grade ethanol, beer, and liquor can all be distilled2. Specific amounts of alcohol can be separated from water in order to create a specific proof2. This process is limited to reducing the percentage of water in the product, but cannot completely eliminate it2. In order to remove water completely, azeotropic distillation is required, which uses extractor chemicals to separate water from ethanol2.
Referências
- About the Refinery." Processing & Refining Crude Oil. Chevron.com, n.d. Web. 17 Nov. 2016.
- Madson, PW. Ethanol Distillation: The Fundamentals. Cincinnati: Katzen International, n.d. Print. Accessed from Web. 01 Oct. 2016.
Transcrição
Understanding the distribution of chemical components in both the vapor and liquid phase, called vapor-liquid equilibrium is essential to the design, operation, and analysis of many engineering processes. Vapor-liquid equilibrium or VLE is a state at which a pure component or mixture exists in both the liquid and vapor phases. The phases are at equilibrium meaning that there were no changes in the macroscopic properties of the system over time. Single component VLE is simple to visualize. Take for example water which is at equilibrium in the vapor and liquid phase at 100 degrees Celsius and one atm. Above this temperature water is a vapor. Below it, water is a liquid. However, engineers generally encounter processes with mixtures in equilibrium making the analysis of VLE more complex and therefore essential to process design. This video will illustrate the principles behind vapor-liquid equilibrium of mixtures and demonstrate how to analyze the VLE of a mixture in the laboratory. Finally, some applications of VLE in the chemical engineering field will be introduced.
When a heated mixture is in a vapor-liquid equilibrium, the vapor and liquid phases generally do not have the same composition. The substance with the lower boiling point will have a higher concentration in the vapor than the substance with the higher boiling point. Thus, engineers refer to components in each phase by their mole fraction where xi is the mole fraction of species i in the liquid and yi is the mole fraction of species i in the vapor phase. This relationship is often depicted using an xy curve like the one shown here for a mixture of two components which illustrates the relationship between each component in each phase. A starting point for all VLE calculations is the simple equilibrium criterion where the fugacity of the species in the vapor equals the fugacity of the species in the liquid. Fugacity is a property related to the exponential difference between the real and ideal gas Gibbs energies. The vapor phase fugacity is equal to the mole fraction of species i in the vapor phase times the pure component vapor fugacity. The expression can be simplified as the pure component vapor fugacity is approximately equal to pressure at low pressure. Liquid phase fugacities are expressed in terms of an activity coefficient, gamma. The activity coefficient is defined as the ratio of a component’s fugacity in an actual mixture to the fugacity of an ideal solution of the same composition. At the saturation vapor pressure the pure component liquid fugacity would equal the saturation vapor pressure because the pure vapor and liquid are in equilibrium there. Finally, since the liquid and vapor fugacities are equal, we can further simplify the relationship as shown which is also known as Raoult’s law. The saturation vapor pressure is often calculated using the Antoine equation where the constants A, B, and C are species-specific and can be found in the literature. Thus, if we measure the compositions of the vapor and liquid which are in equilibrium, we can directly calculate the activity coefficients by measuring temperature and pressure and therefore the saturation vapor pressure. In this experiment a ternary mixture of methanol, isopropyl alcohol and water will be investigated. Various compositions of the mixture are boiled in a VLE apparatus and the lower boiling point components vaporize and are collected in a separate container while the liquid gathers back into the initial sample vessel. Once equilibrium is reached, the liquid and condensed vapor fractions are collected and analyzed with gas chromatography. Using temperature and the liquid and vapor mole fractions the activity coefficients can be calculated. Now that you’ve been introduced to the concepts of VLE and the testing apparatus, let’s see how to carry out the experiment in the laboratory.
To start, drain any liquid out of the system into a waste flask. Keep in mind that the liquid may not completely drain. For the first run add a mixture of 50% methanol, 30% IPA and 20% water through the opening at the top. After filling the mixture, turn on the heater power and condenser water. The apparatus will require roughly 20 minutes to approach equilibrium. The system is now ready to begin the experiment.
When the sample begins boiling, release the stopper to vent the inert outlet of the system. Condensed vapor will start collecting. When equilibrium is reached, steady drips of condensed vapor and returns liquid should be observed. With the temperature stable to within 0.3 degrees for 10 minutes, collect about 1/2 milliliter of liquid in sample vials from both the condensed vapor and the boiling liquid. Drain the condensed vapor from the last sample. Then add a new sample consisting of either 20 milliliters of pure methanol or 50-50 methanol-isopropanol through the sample port. This will give a new overall composition. Reestablish the equilibrium as performed before, however expect a temperature difference from the previous sample. Repeat the equilibration and sampling procedure as before, and then collect the sample to be analyzed. Continue the experiment using different mixtures of the three components. 12 points are sufficient to determine the activity coefficients and the binary interaction coefficients. When all the mixtures have been run, shut down the system by turning off the heaters. When the apparatus begins to cool, shut off the condenser water. Finally measure the composition of each liquid and vapor sample with the gas chromatograph or GC.
Using the system temperature and the liquid and vapor mole fractions acquired from GC, calculate the activity coefficients. This first requires that the saturation pressure is calculated using the Antoine equation where the constants A, B and C for each component can be found in the literature. Now we can use the calculated activity coefficients to correlate the data to a model. We will use the Wilson equation for a ternary mixture which accounts for deviations from ideality in a mixture. The nine lambda constants are the Wilson constants which equal one when i equals j. For each ij pair, there are two different constants. Use a nonlinear regression and a standard sum of squares residual function to determine the six remaining Wilson constants using the mole fraction data from the experiment. The Wilson constants are then used to determine the expected activity coefficients for each component of each sample. Here we show the modeled activity coefficient plotted against the experimental activity coefficients. Ideally, the modeled and experimental activity coefficients would fall along the y equals x line. As you can see in general, the modeled and experimental values fit along this line showing that the model is a good fit to the real system.
Understanding and manipulating the vapor-liquid equilibrium of mixtures is a vital component to a range of processes especially separations. Distillation columns separate mixtures based on their volatility with different compositions of each component in the liquid and vapor phrases on each tray. The more volatile component is vaporized and collected at the top of the column, while the less volatile component remains liquid and is collected at the bottom. VLE data of the components of the mixture is used to determine the number of trays needed to achieve separation in a distillation column. This helps engineers optimize the separation process while keeping operating costs low. Another valuable separation technique using VLE is flash separation. Flash separation is based on the fact that a liquid at a pressure equal to or greater than its bubble point pressure flashes meaning that it partially evaporates when the pressure is reduced. The feed is preheated thus consisting of some liquid and some vapor in equilibrium. It then flows through a pressure reducing valve into the separator. The degree of vaporization and therefore the amount of the solute in the vapor or liquid phases depends on the initial state of the feed stream.
You’ve just watched Jove’s introduction to vapor-liquid equilibrium. You should now understand the concepts behind VLE, how it’s measured in the laboratory, and some of its uses in engineering processes. Thanks for watching.