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Extractive distillation
Extractive distillation
Extractive distillation
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Process flow diagram showing an extractive distillation apparatus. In this case the mixture components A and B are separated in the first column through the solvent E (recovered in the second column).

Extractive distillation is defined as distillation in the presence of a miscible, high-boiling, relatively non-volatile component, the solvent, that forms no azeotrope with the other components in the mixture. The method is used for mixtures having a low value of relative volatility, nearing unity. Such mixtures cannot be separated by simple distillation, because the volatility of the two components in the mixture is nearly the same, causing them to evaporate at nearly the same temperature at a similar rate, making normal distillation impractical.[1]

The method of extractive distillation uses a separation solvent, which is generally non-volatile, has a high boiling point and is miscible with the mixture, but doesn't form an azeotropic mixture. The solvent interacts differently with the components of the mixture thereby causing their relative volatilities to change. This enables the new three-part mixture to be separated by normal distillation. The original component with the greatest volatility separates out as the top product. The bottom product consists of a mixture of the solvent and the other component, which can again be separated easily because the solvent does not form an azeotrope with it. The bottom product can be separated by any of the methods available.

It is important to select a suitable separation solvent for this type of distillation. The solvent must alter the relative volatility by a wide enough margin for a successful result. The quantity, cost and availability of the solvent should be considered. The solvent should be easily separable from the bottom product, and should not react chemically with the components or the mixture, or cause corrosion in the equipment. A classic example to be cited here is the separation of an azeotropic mixture of benzene and cyclohexane, where aniline is one suitable solvent.[2]

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References

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Extractive distillation

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Extractive distillation is a specialized separation technique in chemical engineering used to separate close-boiling-point mixtures or azeotropic mixtures that cannot be effectively resolved by conventional distillation, achieved by introducing a high-boiling, selectively non-volatile solvent (also called an entrainer) that alters the relative volatilities of the components without participating in chemical reactions or forming new azeotropes. This process is particularly valuable for non-ideal mixtures, including minimum or maximum boiling azeotropes and systems with low relative volatility, where the solvent enhances separation efficiency by modifying vapor-liquid equilibrium in a dedicated extractive section of the column. The process typically operates in a continuous mode using at least two columns: the first for extractive , where the feed mixture and are introduced at different points, allowing the more volatile component to be recovered as overhead distillate while the less volatile component and exit the bottom; the second column then regenerates the by stripping it from the bottoms product for . In batch configurations, a single column handles sequential operations, though continuous setups dominate industrial applications due to higher throughput. Key principles include selectivity (measured by the infinite dilution S∞A,BS_{\infty}^{A,B}), ideally greater than 1.2 for effective feasibility, and the use of residue curve maps and univolatility curves to predict separation outcomes and optimize entrainer flow rates, often around 0.5–2 times the feed rate. Common include polar compounds like , N-methylpyrrolidone, or for separations, and more advanced options such as deep eutectic or ionic liquids to reduce demands. Extractive distillation finds widespread application in the chemical, petrochemical, pharmaceutical, and refining industries for producing high-purity products from challenging feeds, such as separating from , from in bioethanol production, or acetone from . Industrial-scale implementations handle hundreds of kilotons per year, with over 50 documented binary mixture separations, and it is especially suited for azeotrope-breaking where alternatives like or pressure-swing methods are less viable. Recent advances emphasize process intensification, including heat-integrated and dividing-wall columns that can reduce energy consumption by up to 50% and capital costs by 23%, alongside eco-friendly solvents like ionic liquids that lower total annual costs (e.g., to $0.73 \times 10^6 for certain systems). First proposed in , it saw early industrial application during for recovering , with significant theoretical advancements in the late , evolving into a cornerstone of modern separation technology.

Principles

Definition and Purpose

Extractive distillation is a specialized separation technique in chemical engineering that involves the addition of a selective solvent, often referred to as an entrainer, to a liquid mixture undergoing distillation. This solvent is typically a high-boiling, relatively non-volatile liquid that is completely miscible with the feed mixture and does not form azeotropes with the components. By interacting preferentially with one or more components in the liquid phase, the solvent alters the relative volatility between the target substances, facilitating their separation in the vapor phase while the solvent itself remains largely in the liquid phase and is recovered separately. The primary purpose of extractive distillation is to overcome limitations of conventional simple distillation, particularly for mixtures exhibiting close boiling points or forming azeotropes, where standard vapor-liquid equilibrium prevents effective . In such cases, the entrainer enhances the differences in volatility without vaporizing significantly, allowing for higher purity separations at potentially lower energy costs compared to alternative methods like . This process is especially valuable in industries requiring precise component isolation, assuming a basic understanding of vapor-liquid equilibrium principles. Extractive distillation emerged in the early as part of advancements in techniques for complex mixtures, with conceptual foundations laid in the amid growing needs in refining to separate hydrocarbons with similar properties. Its industrial viability was solidified through key patents and theoretical developments in the late 1930s and 1940s, including applications for extracting high-purity olefins like during wartime production.

Thermodynamic Basis

Extractive distillation relies on the introduction of a to modify the between components in a , enabling the separation of close-boiling or azeotropic systems that are otherwise difficult to distill. , denoted as αij\alpha_{ij}, is defined as αij=yi/xiyj/xj\alpha_{ij} = \frac{y_i / x_i}{y_j / x_j}, where yiy_i and xix_i are the vapor and mole fractions of component ii, respectively, and similarly for component jj. The selectively interacts with the components, typically reducing the volatility of the more volatile component or enhancing that of the less volatile one, thereby shifting αij>1\alpha_{ij} > 1 to facilitate separation. This modification is crucial for pairs where the native is near unity, as the 's presence alters the vapor- equilibrium (VLE) curve, allowing to proceed without pinch points. The thermodynamic foundation for predicting these lies in non-ideal solution models that account for s, which quantify deviations from ideal behavior in the liquid phase. s γi\gamma_i are functions of temperature TT, pressure PP, and composition, often modeled using equations such as those in the Non-Random Two-Liquid (NRTL) or Universal Quasi-Chemical () frameworks to describe VLE data accurately. In the NRTL model, for instance, ln⁡γi=∑jxjτjiGji∑kxkGki+∑jxjGijτij∑kxkGkj(τji−∑mxmGjmτjm∑kxkGkj)\ln \gamma_i = \sum_j \frac{x_j \tau_{ji} G_{ji}}{\sum_k x_k G_{ki}} + \sum_j \frac{x_j G_{ij} \tau_{ij}}{\sum_k x_k G_{kj}} \left( \tau_{ji} - \sum_m \frac{x_m G_{jm} \tau_{jm}}{\sum_k x_k G_{kj}} \right), where Gij=exp⁡(−αijτij)G_{ij} = \exp(-\alpha_{ij} \tau_{ij}) and τij\tau_{ij} are interaction parameters; similarly uses combinatorial and residual contributions to γi\gamma_i. These models enable the prediction of how the solvent influences ratios γi/γj\gamma_i / \gamma_j, which directly impact via the relation αij=γiPisγjPjs\alpha_{ij} = \frac{\gamma_i P_i^s}{\gamma_j P_j^s} (where PsP^s is saturation ), ensuring reliable simulation and design of extractive processes. For azeotropic mixtures, the solvent disrupts the azeotrope by altering intermolecular interactions, which changes the azeotropic composition and eliminates the vapor-liquid pinch where α=1\alpha = 1. This is achieved through differential solvation effects that shift the equilibrium, preventing the composition where vapor and liquid phases have identical mole fractions. Heavy entrainers, with boiling points significantly higher than those of the target components, are preferred to maintain the solvent predominantly in the phase, minimizing its vaporization and ensuring it acts effectively as a selectivity enhancer without complicating downstream recovery. This phase behavior supports the solvent's role in concentrating at the liquid-vapor interface, promoting efficient during .

Process Description

Operational Steps

The extractive distillation process commences with the introduction of the feed mixture—a typically azeotropic or close-boiling stream—into an intermediate stage of the extractive column, where it is preheated to near its to facilitate efficient . Concurrently, the is introduced at an upper stage, above the feed entry point, to establish an extractive section that promotes intimate contact between the descending liquid and rising vapors without excessive mixing of the feed and streams. This staged addition ensures the selectively alters the relative volatilities of the mixture components throughout the column. In the subsequent countercurrent operation, heat is supplied at the to generate rising vapors enriched in the more volatile component, as the solvent's thermodynamic interaction—such as hydrogen bonding or polarity differences—depresses the volatility of the targeted less volatile . The solvent-laden descends through the column, absorbing and carrying the less volatile component downward, while the vapors progressively purify the more volatile component in the upper sections; this multi-section dynamics (rectifying, extractive, and stripping) maintains steady-state separation under controlled and reboil ratios. The purified more volatile product is then withdrawn as the overhead distillate from the top of the extractive column, often condensed and partially refluxed to enhance purity. The bottoms stream, comprising the less volatile component intimately mixed with the spent solvent, is collected and directed to the subsequent recovery stage. Solvent recovery follows in a dedicated stripper column, where the bottoms from the extractive column are introduced, and steam or direct heating is applied to volatilize and separate the less volatile product overhead, leaving the high-boiling solvent in the bottoms for recycling back to the extractive column; this closed-loop minimizes solvent losses through makeup streams. Mass balance considerations are critical, with the solvent-to-feed ratio typically ranging from 1:1 to 10:1 by weight, selected to achieve desired product purities (e.g., >99%) while optimizing energy efficiency and column throughput.

Equipment and Configuration

The main extractive column in an extractive distillation process is typically a multi-stage or packed column designed to facilitate the separation of close-boiling or azeotropic mixtures through the addition of a selective . These columns generally require 20-100 theoretical plates to achieve the desired purity, depending on the mixture's and separation difficulty. The is introduced via a dedicated feed positioned above the main feed , typically in the upper third of the column, to ensure it descends countercurrently through the mixture without premature volatilization and to maximize its extractive effect in the stripping section below. A secondary stripper column is employed for solvent regeneration, receiving the bottoms stream from the main extractive column and operating at reduced or with reboiling to separate the from the heavy key component. This unit typically achieves greater than 99% recovery, enabling its recycle to the main column while minimizing losses and operational costs. The is often a simpler or packed column with fewer stages than the main unit, focused on high-purity reclamation. Heat integration is essential for efficiency, incorporating condensers to cool overhead vapors, to generate rising vapors, and pumps for transfer between columns. Due to the dual-column setup and higher circulation, the total energy input is higher than that of simple for separable mixtures, primarily from increased duties, though optimizations like networks can mitigate this. Control systems monitor profiles across key trays to maintain solvent selectivity and prevent deviations in composition, often using PID controllers or advanced neural networks for real-time adjustments to ratios and feed flows. Safety features, such as relief valves and corrosion-resistant materials, address the handling of high-boiling solvents that may cause or thermal degradation. Industrial-scale columns measure 1-5 meters in , capable of processing 100-1000 tons per day, supporting large-volume operations like aromatic recovery.

Solvent Selection

Criteria for Solvents

In extractive distillation, the primary criterion for solvent selection is selectivity, which refers to the 's ability to preferentially interact with one component of the mixture over the other, thereby altering the to facilitate separation. This preferential interaction often occurs through mechanisms such as hydrogen bonding or differences in polarity, which disrupt the interactions in the original or close-boiling mixture. Selectivity is quantitatively measured by the parameter S=(γ2/γ1)solvent(γ2/γ1)pureS = \frac{(\gamma_2 / \gamma_1)_{\text{solvent}}}{(\gamma_2 / \gamma_1)_{\text{pure}}}, where γ\gamma denotes the of components 1 and 2; values significantly greater than 1 indicate effective enhancement of relative volatility. Selectivity is quantitatively measured by the infinite dilution selectivity S∞A,B=γ∞Bγ∞AS_{\infty}^{A,B} = \frac{\gamma_{\infty}^B}{\gamma_{\infty}^A}, where A is the more volatile component and B the less volatile; typical feasible values exceed 1.05–1.4, though lower values (e.g., ~0.8) can enable separation with higher flows and process optimization. Solvency requirements emphasize the solvent's capacity to dissolve the target components while minimizing mutual with the separated products to simplify downstream recovery. High is characterized by a large , such as C∞=1/γ∞C^\infty = 1 / \gamma^\infty, reflecting strong solute-solvent interactions at infinite dilution. Additionally, the solvent's should be 50-100°C higher than that of the mixture's highest-boiling component to ensure it remains predominantly in the liquid phase during , reducing entrainment losses. Solvents must exhibit thermal and chemical stability under operating conditions, typically up to 200-250°C, to prevent decomposition that could contaminate the products or require frequent replacement. They should also be non-corrosive to equipment materials, non-toxic for handling and environmental compliance, and recyclable without significant degradation to maintain process efficiency over multiple cycles. Economic viability is crucial, with the solvent cost ideally comprising less than 5% of the product value to avoid undermining the overall process profitability. Low vapor pressure is essential to minimize solvent losses in the overhead vapor, often quantified by a Henry's law constant exceeding 10 atm to limit volatilization. Solvent candidates are evaluated through laboratory vapor-liquid equilibrium (VLE) measurements to determine activity coefficients and phase behavior experimentally, followed by process simulations using software like Aspen Plus to predict performance, optimize flows, and estimate total annual costs.

Common Solvents and Properties

Sulfolane (tetramethylene sulfone) is one of the most widely used solvents in extractive due to its high of 285°C and of 1.26 g/cm³ at 25°C, which facilitate its recovery by without excessive energy input. With a molecular weight of 120.17 g/mol and low toxicity, sulfolane exhibits excellent selectivity for separating aromatics from aliphatics, such as in benzene-toluene-xylene (BTX) extraction, where it preferentially solvates aromatic hydrocarbons while showing low for non-aromatics. Its stability up to 250°C and non-corrosive nature make it suitable for industrial-scale operations. N-Methylpyrrolidone (NMP), a with a of 202°C and viscosity of 1.7 cP at 25°C, is effective for separations involving polar mixtures, including alcohol-water systems. Its molecular weight is 99.13 g/mol, and it provides good solvency for organics while being recoverable via . However, NMP is subject to environmental regulations due to potential and persistence in the environment. It demonstrates selectivity in reversing relative volatilities for azeotropic mixtures like isopropanol-water. Ethylene glycol (EG), with a of 197°C and molecular weight of 62.07 g/mol, serves as a cost-effective for processes, offering high solvency for and hydrocarbons in alcohol- separations. Its density is 1.113 g/cm³ at 25°C, but it can pose risks to equipment, necessitating or alloy construction. EG enhances the of over , with an infinite dilution selectivity (S∞S_{\infty}) of approximately 1.62 for the - pair. Glycerol, a natural and biodegradable , has a high of 290°C and molecular weight of 92.09 g/mol, making it suitable for biofuel-related separations where is prioritized. Despite its high of 1.5 Pa·s at 25°C, which can impact , glycerol effectively breaks azeotropes in ethanol-water mixtures (S∞ethanol/water=0.81S_{\infty}^{ethanol/water} = 0.81), though its lower selectivity requires higher entrainer flows or mixed systems for optimal performance. Its renewability and low cost derive from byproducts. Emerging solvents such as ionic liquids (ILs) and deep eutectic solvents (DES) are gaining prominence for their tunability, negligible , and high selectivity (often >1.5 for aromatic/aliphatic or alcohol/ systems). For example, ILs like [bmim][BF4] offer thermal stability up to 300°C and reduced energy use by 20-30% in simulations, while DES (e.g., choline chloride-urea) provide biodegradable alternatives with selectivities around 1.2-2.0 for ethanol-, lowering costs to ~$0.73 \times 10^6 annually for certain processes as of 2023. These are evaluated similarly via VLE data but prioritized for eco-compliance.
SolventBoiling Point (°C)Molecular Weight (g/mol)Selectivity Index Example
Sulfolane285120.17High for aromatics/aliphatics (e.g., benzene/heptane ~12 at infinite dilution)
N-Methylpyrrolidone20299.13Suitable for alcohol/water (reverses volatility in isopropanol/water)
19762.07S∞=1.62S_{\infty} = 1.62 (ethanol/water)
29092.09S∞=0.81S_{\infty} = 0.81 (ethanol/water)

Applications

Industrial Processes

In the , extractive distillation is a cornerstone process for separating aromatic hydrocarbons like and from aliphatic impurities in reformate streams derived from units. A selective solvent, such as or N-methylpyrrolidone, is introduced to the distillation column to selectively enhance the of the aromatics, allowing their extraction as overhead products while non-aromatics exit as bottoms. This integration with upstream reforming and downstream purification steps enables efficient recovery of , , and xylenes (BTX), which are vital feedstocks for polymers, solvents, and fuels. A significant portion of global BTX production, with approximately 70% of derived from extraction-based methods including extractive distillation from reformate or gasoline streams. In ethanol production, extractive distillation addresses the ethanol-water azeotrope at 95.6 wt% , enabling the production of fuel-grade (>99.5 wt%) suitable for blending in . High-boiling solvents like or are added to shift the , dehydrating the fermented broth in a dedicated column integrated downstream of conventional and units. This process has been incorporated into plants, supporting scalable output by combining with upstream conversion and downstream blending operations. For fine chemicals , extractive distillation purifies high-value solvents such as from aqueous impurities or -forming mixtures, yielding products with >99.9% purity for use in pharmaceuticals, , and . Entrainer solvents like break the -water in a multi-column setup, with the process scaled to smaller capacities of 10-1000 tons per year to match batch-oriented production. Integration with waste recovery streams enhances in specialty chemical facilities. In chemical , extractive distillation also separates acetone from using solvents like or . Across these applications, extractive distillation typically requires 20-50% higher energy input than simple distillation owing to the additional column for solvent recovery and higher ratios, yet it uniquely enables separations unattainable by conventional means, such as breaking or close-boiling mixtures.

Specific Case Studies

One prominent implementation of extractive distillation is the UOP ™ process, widely adopted for recovering high-purity and from reformate splitter overhead or hydrotreated gasoline feeds containing 60-80% aromatics. In this process, serves as the selective solvent, introduced at the upper section of the extractive distillation column to alter relative volatilities, enabling separation of aromatics from non-aromatics like paraffins and naphthenes. The process achieves purity of 99.9 wt% (meeting ASTM Refined -545 specifications) and purity exceeding 99.95 wt% with less than 1000 wt-ppm non-aromatics, while typical raffinate non-aromatics exceed 98 vol%. UOP has licensed over 100 such units globally since the , with individual plant capacities often processing hundreds of thousands of tons per year; for instance, a commercial unit in Hainan Refinery, , operates at 100,000 tons/year of with 99.99% purity and 99.67% recovery. is approximately 275-300 kcal per kg of extract produced, reflecting efficient solvent circulation and minimal degradation, with solvent losses below 5 ppm of feed rate. Another key application is the dehydration of to produce bioethanol, particularly in Brazilian industrial where extractive distillation has been operational since the late 1990s to overcome the ethanol-water . Using glycols such as or as entrainers, the process involves feeding the near the top of the extractive column to selectively enhance volatility, followed by recovery in a stripper column. By 2003, over 20 such were operational in , accounting for about 25% of the country's production (approximately 1.5 billion liters annually from these ), with additional capacity expansions adding 360 million liters/year. These implementations achieve purity of 99.5-99.9 vol%, with yields exceeding 98%, and demonstrate 15-20% reductions compared to traditional azeotropic methods through optimized integration and lower ratios (typically 1.5-2.0). , a byproduct, is particularly favored in for its availability and low volatility, enabling operational stability and recycling rates above 99%, with processing up to 500,000 liters/day of hydrous feed. Recent innovations focus on replacing traditional solvents with ionic liquids (ILs) as greener alternatives, offering lower volatility, higher selectivity, and reduced environmental impact. Piloted in the for separations like benzene-toluene-xylene from pyrolysis gasoline and , IL-based extractive distillation has demonstrated 10-15% lower energy use than systems in lab-to-pilot scales, with purities up to 99.5% and minimal solvent losses (<0.1 wt%). For instance, [EMIM][OAc] IL pilots for BTX separation achieve >99% yield, while refrigerant pilots using [C1C2im][Tf2N] confirm scalability for industrial retrofits by 2030. These advancements prioritize tunable IL properties for specific feeds, enhancing overall process .

Advantages and Limitations

Key Benefits

Extractive distillation enables the separation of azeotropic mixtures and close-boiling components, where conventional is inefficient and requires excessive stages to achieve high purities. By introducing a selective that alters relative volatilities without forming new azeotropes, the process overcomes limitations of simple vapor-liquid equilibrium, allowing effective rectification of non-ideal systems like ethanol-water or acetone-methanol. The technique offers high selectivity, routinely achieving product purities exceeding 99% in a single pass, which minimizes the need for additional purification steps and enhances overall process efficiency. This level of precision is particularly valuable in industries requiring ultra-high purity outputs, such as pharmaceuticals and petrochemicals. Solvent recyclability is a core advantage, with recovery rates often surpassing 99%, which significantly reduces waste generation and operational expenses by limiting solvent makeup to less than 1% of total costs. In practical applications, nearly complete solvent regeneration via a dedicated stripping column ensures sustainable operation and low environmental impact. The process demonstrates versatility for handling heat-sensitive materials, operating at moderate temperatures typically ranging from 100-200°C, which preserves compound integrity compared to higher-temperature alternatives. This is evident in cases like glycerol-based separations, where controlled thermal conditions prevent degradation. Economically, capital costs are higher than those of simple columns due to the additional recovery unit, but the investment yields rapid payback through increased throughput and energy-efficient designs that lower total annual costs by 20-30%.

Challenges and Drawbacks

Extractive distillation's dual-column configuration results in significantly higher compared to simpler methods like flash distillation, typically requiring 50-100% more energy due to the additional and condenser duties in the solvent recovery column. This elevated demand contributes to increased operational costs and . Mitigation through heat integration and multi-effect distillation can achieve energy savings of up to 45%, enhancing overall efficiency. Recent advances, such as the use of ionic liquids, can further reduce by up to 50%. Solvent handling presents risks of degradation or contamination, which can lead to off-specification products, column fouling, and reduced separation efficiency. For instance, solvents like degrade under high temperatures or oxidative conditions, introducing impurities that affect downstream processes. These issues are addressed by implementing solvent purification loops and regular monitoring to regenerate and recycle the entrainer effectively. The process exhibits high capital intensity, with initial investments often 20-50% greater than conventional owing to the need for larger extractive columns, additional recovery equipment, and auxiliary systems for solvent circulation. This upfront cost can delay project viability, particularly in retrofit applications. Environmental concerns stem from the use of certain solvents, such as N-methylpyrrolidone (NMP), which is a associated with and reproductive risks, prompting regulatory actions like EPA restrictions under TSCA since the to limit exposure and emissions. In response, there has been a shift toward bio-based alternatives post-2010 regulations, offering lower environmental impact while maintaining selectivity. Operational complexity arises from the process's sensitivity to feed variations, such as changes in composition or flow rate, which can destabilize the separation and require precise adjustments to maintain purity. Advanced control strategies, including dual reflux-to-feed ratio controllers across columns, are employed to enhance robustness and minimize disruptions.

Comparisons

With Azeotropic Distillation

Extractive distillation and azeotropic distillation both serve as enhanced separation techniques for overcoming azeotropic limitations in binary or multicomponent mixtures, but they differ fundamentally in their mechanisms. In extractive distillation, a high-boiling, relatively non-volatile solvent is introduced into the distillation column, where it interacts primarily with the liquid phase to selectively alter the relative volatilities of the components without forming a new azeotrope; the solvent remains largely in the bottoms product due to its low volatility, facilitating the enrichment of the more volatile component in the distillate. In contrast, azeotropic distillation employs a volatile entrainer that mixes with the feed to create a temporary, lower-boiling azeotrope, which carries components across the original azeotropic boundary into the vapor phase for separation. The processes also diverge in configuration and operation. Extractive distillation typically requires a dual-column setup: the primary column performs the extractive separation with the solvent fed near the top to establish an extractive section, while a secondary stripper column recovers the solvent from the bottoms for recycling, minimizing losses and enabling continuous operation. Azeotropic distillation, however, often utilizes a single main column where the entrainer is added with or near the feed, producing a heteroazeotropic overhead that undergoes phase separation in a decanter to yield distinct organic and aqueous layers, which are then recycled or further processed; this can involve additional columns for entrainer recovery but avoids a dedicated extractive section. For instance, in ethanol dehydration, extractive distillation with ethylene glycol requires 22 stages in the main column and 32 in the recovery column, whereas azeotropic distillation with cyclohexane uses 30 stages in the main column plus a decanter and 25 stages in recovery. Applications of the two methods target distinct mixture types based on their mechanisms. Extractive distillation excels in separating non-ideal, close-boiling mixtures or minimum-boiling azeotropes, such as - or ethanol-water systems, where the heavy solvent enhances selectivity without volatility interference. is more suited to aqueous or polar systems like tetrahydrofuran-water or ethanol-water, where the entrainer's volatility aids in forming a separable heteroazeotrope, as seen in industrial dehydration processes using or . Regarding advantages and limitations, extractive distillation provides superior control over separation by preventing azeotrope reformation through the solvent's liquid-phase action, often resulting in lower overall energy demands—such as 59% less reboiler duty compared to azeotropic methods in purification—and reduced total annual costs by up to 39%. However, it incurs higher energy penalties from solvent recovery and requires careful solvent handling to avoid contamination. Azeotropic distillation offers a simpler, more compact setup with fewer stages in some configurations, but it is constrained by entrainer purity requirements, potential volatility losses, and significantly higher due to the need for phase splitting and handling flammable volatiles. Historically, emerged earlier in the early for applications like alcohol dehydration, predating widespread industrial adoption. Extractive distillation, while conceptualized around the same period, achieved larger-scale implementation in the post-World War II era, driven by demands for aromatic separations and supported by advancements in solvent technology like the Udex process.

With Conventional Distillation

Conventional distillation, also known as , separates liquid mixtures based on the inherent differences in the volatility of their components, quantified by the (α), which must typically exceed about 1.05 for large-scale industrial applications. In contrast, extractive distillation is employed when these natural volatility differences are insufficient, such as when α approximates 1, by introducing a selective that interacts preferentially with one component to artificially enhance the relative volatility and enable separation. This solvent addition alters the thermodynamic behavior in the liquid phase without significantly affecting the vapor phase, allowing the process to overcome limitations inherent to conventional methods. The setup for conventional distillation involves a single distillation column where the feed is introduced, and separation occurs through repeated and across 10–30 theoretical stages, depending on the and desired purity. Extractive distillation, however, requires a more complex arrangement: the is added to the upper section of the primary column to create an extractive section, often requiring 20–40 stages in that column, followed by a second column for recovery and recycling. This dual-column configuration increases capital investment and operational complexity compared to the straightforward single-column design of conventional . Conventional distillation becomes infeasible for mixtures forming azeotropes, where the relative volatility reaches unity at a specific composition, preventing further purification beyond the azeotropic point—for instance, the ethanol-water system at 95.6 wt% ethanol cannot be dehydrated further without additional measures. Extractive distillation addresses this by selecting a solvent that breaks the azeotrope, such as ethylene glycol for ethanol-water, enabling high-purity recovery, though at higher cost due to the extra equipment and processing steps. In terms of efficiency, conventional distillation benefits from its and generally lower duties compared to extractive methods. Extractive distillation, while effective for challenging separations, demands higher energy primarily from the solvent recovery column, making it viable primarily for high-value products where alternative methods are impractical. This added energy penalty is justified in scenarios like pharmaceutical intermediates, but it underscores the in selecting extractive over conventional approaches. Conventional distillation has been a universal technique since the , evolving with industrial-scale fractional columns for and applications. Extractive distillation emerged as a niche solution in the , particularly for addressing azeotropic challenges in emerging processes, with early patents dating to 1923 and significant adoption post-World War II for aromatic hydrocarbon separations.

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