The document discusses the design of a Karr reciprocating-plate extractor (T-102) for a liquid-liquid extraction process in a biodiesel production plant. Key details include:
- Methanol will be used as the key component for the extractor design due to its solubility in both the feed and solvent streams.
- Design calculations are provided for the methanol recovery, distribution coefficient, continuous phase flux, and mass fraction of methanol in the raffinate stream.
- The operating feed to minimum solvent flow rate ratio is calculated as 2.2 based on the methanol distribution coefficient and mass fractions. This ratio is used to determine the minimum solvent flow rate of 2775.08 kg/h for
The document describes the design of a Karr reciprocating-plate extractor to separate a mixture of methylene chloride and methanol. The extractor is designed to separate a feed with mass flow rates of 2185 lb/h of methylene chloride and 33 lb/h of methanol, using water as the selective solvent at a mass flow rate of 2218 lb/h, to recover 95% of the methanol. The design process involves calculating the mass fractions, minimum solvent flow rate, extraction factor, number of equilibrium stages, and diameter and height of the extractor. The calculated diameter and height of the designed extractor are 10.42 inches and 7 feet, respectively.
The document summarizes the design of an absorption column to remove SO2 from an air stream using water. It involves selecting water as the solvent, 1.5 inch Raschig rings as the packing material, calculating the minimum water flow rate of 116,641 kg/h, determining the flooding velocity, diameter of 1.106 m, and height of 3.88 m for the packed column. The column will treat 40,000 ft3/h of air containing 20% SO2 and recover 96% of the SO2 using 30% excess water than the minimum flow rate.
The document provides an overview of unit operations in chemical engineering. It defines unit operations as basic steps that involve physical changes like separation, crystallization, evaporation. Examples of common unit operations are given like heat transfer, evaporation, drying, absorption. Different types of unit operations are classified. Key aspects of specific unit operations like heat transfer, drying, evaporation and distillation are described in further detail. The document highlights the importance of understanding the physical laws governing each unit operation for effective analysis and design of chemical processes.
This document discusses a project on studying the steam economy of a multiple effect evaporator plant that produces sodium sulfate. It is a report submitted by 4 students to fulfill their Bachelor of Engineering degree requirements. The project aims to determine why steam utility increases over time in the plant's multiple effect evaporator for sodium sulfate production and find a suitable solution to reduce it. It will also involve simulating the multiple effect evaporator process using Excel. The document provides background on evaporators, multiple effect evaporators, sodium sulfate and its applications.
In most chemical engineering curriculums, distillation and liquid-liquid extraction (LLE) do not receive equal billing. Yet, this powerful separations technology is in place across the CPI, pharmaceutical and oil/gas industries. Discover how to design an LLE column with industry experts Don Glatz and Brendan Cross as they discuss specific examples and separations challenges.
Extraction theory involves removing soluble materials from insolids using liquid solvents. Liquid-liquid extraction is a useful method to separate components of a mixture based on differences in solubility between solvents. For example, sugar can be extracted from vegetable oil by shaking the mixture with water, as sugar is more soluble in water than oil. The partition coefficient K quantifies differences in solubility, with some compounds made more water-soluble by conversion to ionic salt forms using acid or base treatment. This allows separation of organic acid/base mixtures based on differing solubility properties.
Chemical reaction engineering involves designing chemical reactors to optimize reaction rates and yields. There are several factors that influence reaction rates, including concentration, temperature, and catalysts. Common reactor types include batch, continuous stirred-tank (CSTR), and plug flow reactors. Reactors can be run in series or parallel to improve conversion levels. Residence time distribution is important for understanding flow patterns within real reactors.
The document describes the design of a Karr reciprocating-plate extractor to separate a mixture of methylene chloride and methanol. The extractor is designed to separate a feed with mass flow rates of 2185 lb/h of methylene chloride and 33 lb/h of methanol, using water as the selective solvent at a mass flow rate of 2218 lb/h, to recover 95% of the methanol. The design process involves calculating the mass fractions, minimum solvent flow rate, extraction factor, number of equilibrium stages, and diameter and height of the extractor. The calculated diameter and height of the designed extractor are 10.42 inches and 7 feet, respectively.
The document summarizes the design of an absorption column to remove SO2 from an air stream using water. It involves selecting water as the solvent, 1.5 inch Raschig rings as the packing material, calculating the minimum water flow rate of 116,641 kg/h, determining the flooding velocity, diameter of 1.106 m, and height of 3.88 m for the packed column. The column will treat 40,000 ft3/h of air containing 20% SO2 and recover 96% of the SO2 using 30% excess water than the minimum flow rate.
The document provides an overview of unit operations in chemical engineering. It defines unit operations as basic steps that involve physical changes like separation, crystallization, evaporation. Examples of common unit operations are given like heat transfer, evaporation, drying, absorption. Different types of unit operations are classified. Key aspects of specific unit operations like heat transfer, drying, evaporation and distillation are described in further detail. The document highlights the importance of understanding the physical laws governing each unit operation for effective analysis and design of chemical processes.
This document discusses a project on studying the steam economy of a multiple effect evaporator plant that produces sodium sulfate. It is a report submitted by 4 students to fulfill their Bachelor of Engineering degree requirements. The project aims to determine why steam utility increases over time in the plant's multiple effect evaporator for sodium sulfate production and find a suitable solution to reduce it. It will also involve simulating the multiple effect evaporator process using Excel. The document provides background on evaporators, multiple effect evaporators, sodium sulfate and its applications.
In most chemical engineering curriculums, distillation and liquid-liquid extraction (LLE) do not receive equal billing. Yet, this powerful separations technology is in place across the CPI, pharmaceutical and oil/gas industries. Discover how to design an LLE column with industry experts Don Glatz and Brendan Cross as they discuss specific examples and separations challenges.
Extraction theory involves removing soluble materials from insolids using liquid solvents. Liquid-liquid extraction is a useful method to separate components of a mixture based on differences in solubility between solvents. For example, sugar can be extracted from vegetable oil by shaking the mixture with water, as sugar is more soluble in water than oil. The partition coefficient K quantifies differences in solubility, with some compounds made more water-soluble by conversion to ionic salt forms using acid or base treatment. This allows separation of organic acid/base mixtures based on differing solubility properties.
Chemical reaction engineering involves designing chemical reactors to optimize reaction rates and yields. There are several factors that influence reaction rates, including concentration, temperature, and catalysts. Common reactor types include batch, continuous stirred-tank (CSTR), and plug flow reactors. Reactors can be run in series or parallel to improve conversion levels. Residence time distribution is important for understanding flow patterns within real reactors.
This document outlines the procedures and results from an experiment on gas absorption using an absorption column. The experiment examined the air pressure drop across the column as air flow rate was increased for different fixed water flow rates. Pressure drop was recorded and plotted against air flow rate. The experimental flooding points where compared to theoretical calculations, with errors ranging from 11.1% to 20%. The results showed that pressure drop increased with air flow rate as expected, identifying the flooding points where liquid could no longer flow down the column.
An overview of distillation column design concepts and major design considerations. Explains distillation column design concepts, what you would provide to a professional distillation column designer, and what you can expect back from a distillation system design firm. To speak with an engineer about your distillation column project, call EPIC at 314-207-4250.
- This document describes absorption and stripping processes using packed columns and graphical methods.
- It discusses operating lines, height of transfer units (HOG), number of transfer units (NOG), and how to calculate the height equivalent of a theoretical plate (HETP) for a packed column given mass transfer coefficients, flow rates, and equilibrium data.
- An example is provided to calculate the HETP for a specific packed column based on the mass transfer coefficients, flow rates, and equilibrium constant given.
Packed columns are used for distillation, gas absorption, and liquid-liquid extraction. They have continuous gas-liquid contact through a packed bed, unlike plate columns which have stage-wise contact. Packed columns depend on good liquid and gas distribution, and have lower holdup but higher pressure drop than plate columns. This document provides details on packed column components, design procedures such as selecting packing and determining height, and examples of absorption and stripping processes in packed columns.
I found no good source for extractive distillation on the internet.So i decided to make one myself.This ppt discusses about the technology,its working and benefits.It compares extractive distillation side by side to azeotropic distillation and counts the advantages.
Types of Distillation & column internalsBharat Kumar
More:- https://chemicalengineeringworld.com
Distillation is a method of separating the components of a solution which depends upon distribution of the substances between a gas and liquid phase, applied to cases where all components are present in both phases.
* What is distillation ?
* Types of Distillation
* Batch Distillation
* Azeotropic Distillation
* Flooding
* Priming
* Coning
* Weeping
* Dumping
* Packed Column
* Tray column
* Reflux Ratio
* Relative volatility
* Distillation column
Distillation is a method of separating mixtures based on differences in volatility (volatility is the tendency of a substance to vaporize. Volatility is directly related to a substance's vapor pressure.) of components in a boiling liquid mixture. Distillation is a unit operation, or a physical separation process, and not a chemical reaction
This document discusses packed columns for distillation. It begins with an introduction to distillation and the types of distillation columns. It then focuses on packed columns, describing their components, types of packing materials and packing, design procedures, and methods for calculating packing height. It also covers applications of packed columns, advantages and disadvantages compared to tray columns, and examples of packed column usage.
Armfield Gas Absorption Column ExperimentHadeer Khalid
The absorption of CO2 from air to water was studied in Gas absorption column built by Armfield company. Lab report and experiment was part of Separation Lab.
The document discusses evaporator performance and factors that affect it. It explains that the boiling point of solutions is higher than water alone, known as boiling point elevation. It also discusses how capacity, economy, and steam consumption are measures of evaporator performance. Capacity is the amount of water vaporized per hour, economy is the amount vaporized per unit of steam, and steam consumption can be estimated from capacity and economy. Duhring's rule and boiling point elevation must be considered for heat transfer calculations in evaporators dealing with solutions.
This document contains Antoine coefficients for various compounds. The Antoine coefficients relate the log of vapor pressure (P) of a compound to temperature (T) using the formula log(P) = A-B/(T+C). The table lists over 100 compounds along with their Antoine coefficients (A, B, C values) and temperature ranges of applicability.
The McCabe-Thiele method is a graphical technique for determining the minimum number of stages required for distillation. It involves plotting the equilibrium relationship between liquid and vapor phases on a diagram and constructing operating lines to represent the mass balances in the rectifying and stripping sections. Intersections between the lines indicate the number of ideal stages. The method was developed in 1925 and remains useful for preliminary column design. Key considerations include the feed composition and enthalpy, reflux ratio, and use of partial condensers or reboilers.
1. Agitation involves inducing motion within a material while mixing distributes components randomly.
2. Mixing operations involve various combinations of gases, liquids, and solids and may require agitation to enhance mass and heat transfer between phases.
3. Effective agitation and mixing depends on factors like the impeller type, liquid properties, and vessel design which influence flow patterns within the vessel.
Perforated plate column - LLE EquipmentFawad Akram
Perforated plate columns are used for liquid-liquid extraction. They consist of several perforated plates along with downcomers or upcomers for the continuous phase. Mass transfer occurs as the dispersed phase forms droplets on the plates and moves countercurrently between stages. Engineers can design perforated plate columns using rate equations to model mass transfer and locate a pseudoequilibrium curve, which is then used with an operating line to determine the required number of stages. The design procedure involves iteratively guessing composition values to calculate flow rates and ensure they match at equilibrium.
wholw Content is covered in this presentation .it will give u a basic idea and types about leaching and it will also provide u information via Diagrams .
This document provides an overview of distillation concepts and methods. It discusses general principles of continuous distillation operations and related separation processes. Various thermodynamic models, data correlations, and methods for analyzing distillation columns are presented, including graphical and rigorous computational approaches. Enhanced distillation techniques like azeotropic distillation and extractive distillation are also covered to facilitate separations involving azeotropes or close-boiling components.
Gas absorption is a process used to separate gases by contacting a gas mixture with a liquid solvent. The key principles are the solubility of the absorbed gas and the rate of mass transfer as the gas dissolves into the liquid. Absorption is usually carried out counter-currently in vertical columns. The solvent is fed at the top while the gas enters at the bottom, allowing the absorbed substances to be washed out in the downward flowing liquid. Proper selection of solvent considers factors like gas solubility, volatility, cost, and viscosity. Rate of absorption is determined by volumetric mass transfer coefficients, which can be calculated from operating line and equilibrium curve diagrams.
This document discusses the McCabe Thiele method for calculating multistage separation processes. It provides examples of how to use the method graphically to determine the number of theoretical stages, flow rates, and other parameters. Specifically, it discusses how to: 1) draw equilibrium curves and operating lines to determine minimum reflux ratio and feed location; 2) calculate flow rates, number of stages, and utilities using material balances; and 3) handle special cases like multiple feeds, enriched/stripped sections, and side product specifications. An example problem demonstrates applying these steps to design a binary distillation column with two feed streams.
it is a mass transfer operation use in chemical industries
it is a simple diffusion of solid to liquid phase and foam a new concentrate liquid solution
it is base on simple diffusion how to work in industries this operation
it is use for pharma, seeds and oil industries.
This document summarizes a student project to determine the damping coefficient of SAE20W50 engine oil mixed with activated carbon from coconut shells (biochar). Experiments were conducted using a Universal Vibration Apparatus to measure the damping coefficient of the oil-biochar mixtures and pure SAE20W50 oil. The damping coefficient increased as the percentage of biochar added to the oil increased, with the highest damping observed for a 15% biochar mixture. The results show that adding biochar can improve the damping properties of SAE20W50 engine oil.
Method 8260C by Purge and Trap Gas Chromatography Mass Spectrometry using the...PerkinElmer, Inc.
The document describes a study evaluating the performance of a PerkinElmer Clarus SQ 8 GC/MS using EPA Method 8260C for analyzing volatile organic compounds. Key findings include:
1) The GC/MS system met or exceeded all Method 8260C performance criteria for calibration, detection limits, precision, and accuracy when analyzing 31 volatile organic compounds.
2) Detection limits were as low as 0.05 μg/L and precision and accuracy were within accepted ranges of 76-109% and 0.9-7.4%, respectively.
3) The fast cooling GC oven and high throughput of the system allowed analysis times of under 30 minutes between samples.
This document outlines the procedures and results from an experiment on gas absorption using an absorption column. The experiment examined the air pressure drop across the column as air flow rate was increased for different fixed water flow rates. Pressure drop was recorded and plotted against air flow rate. The experimental flooding points where compared to theoretical calculations, with errors ranging from 11.1% to 20%. The results showed that pressure drop increased with air flow rate as expected, identifying the flooding points where liquid could no longer flow down the column.
An overview of distillation column design concepts and major design considerations. Explains distillation column design concepts, what you would provide to a professional distillation column designer, and what you can expect back from a distillation system design firm. To speak with an engineer about your distillation column project, call EPIC at 314-207-4250.
- This document describes absorption and stripping processes using packed columns and graphical methods.
- It discusses operating lines, height of transfer units (HOG), number of transfer units (NOG), and how to calculate the height equivalent of a theoretical plate (HETP) for a packed column given mass transfer coefficients, flow rates, and equilibrium data.
- An example is provided to calculate the HETP for a specific packed column based on the mass transfer coefficients, flow rates, and equilibrium constant given.
Packed columns are used for distillation, gas absorption, and liquid-liquid extraction. They have continuous gas-liquid contact through a packed bed, unlike plate columns which have stage-wise contact. Packed columns depend on good liquid and gas distribution, and have lower holdup but higher pressure drop than plate columns. This document provides details on packed column components, design procedures such as selecting packing and determining height, and examples of absorption and stripping processes in packed columns.
I found no good source for extractive distillation on the internet.So i decided to make one myself.This ppt discusses about the technology,its working and benefits.It compares extractive distillation side by side to azeotropic distillation and counts the advantages.
Types of Distillation & column internalsBharat Kumar
More:- https://chemicalengineeringworld.com
Distillation is a method of separating the components of a solution which depends upon distribution of the substances between a gas and liquid phase, applied to cases where all components are present in both phases.
* What is distillation ?
* Types of Distillation
* Batch Distillation
* Azeotropic Distillation
* Flooding
* Priming
* Coning
* Weeping
* Dumping
* Packed Column
* Tray column
* Reflux Ratio
* Relative volatility
* Distillation column
Distillation is a method of separating mixtures based on differences in volatility (volatility is the tendency of a substance to vaporize. Volatility is directly related to a substance's vapor pressure.) of components in a boiling liquid mixture. Distillation is a unit operation, or a physical separation process, and not a chemical reaction
This document discusses packed columns for distillation. It begins with an introduction to distillation and the types of distillation columns. It then focuses on packed columns, describing their components, types of packing materials and packing, design procedures, and methods for calculating packing height. It also covers applications of packed columns, advantages and disadvantages compared to tray columns, and examples of packed column usage.
Armfield Gas Absorption Column ExperimentHadeer Khalid
The absorption of CO2 from air to water was studied in Gas absorption column built by Armfield company. Lab report and experiment was part of Separation Lab.
The document discusses evaporator performance and factors that affect it. It explains that the boiling point of solutions is higher than water alone, known as boiling point elevation. It also discusses how capacity, economy, and steam consumption are measures of evaporator performance. Capacity is the amount of water vaporized per hour, economy is the amount vaporized per unit of steam, and steam consumption can be estimated from capacity and economy. Duhring's rule and boiling point elevation must be considered for heat transfer calculations in evaporators dealing with solutions.
This document contains Antoine coefficients for various compounds. The Antoine coefficients relate the log of vapor pressure (P) of a compound to temperature (T) using the formula log(P) = A-B/(T+C). The table lists over 100 compounds along with their Antoine coefficients (A, B, C values) and temperature ranges of applicability.
The McCabe-Thiele method is a graphical technique for determining the minimum number of stages required for distillation. It involves plotting the equilibrium relationship between liquid and vapor phases on a diagram and constructing operating lines to represent the mass balances in the rectifying and stripping sections. Intersections between the lines indicate the number of ideal stages. The method was developed in 1925 and remains useful for preliminary column design. Key considerations include the feed composition and enthalpy, reflux ratio, and use of partial condensers or reboilers.
1. Agitation involves inducing motion within a material while mixing distributes components randomly.
2. Mixing operations involve various combinations of gases, liquids, and solids and may require agitation to enhance mass and heat transfer between phases.
3. Effective agitation and mixing depends on factors like the impeller type, liquid properties, and vessel design which influence flow patterns within the vessel.
Perforated plate column - LLE EquipmentFawad Akram
Perforated plate columns are used for liquid-liquid extraction. They consist of several perforated plates along with downcomers or upcomers for the continuous phase. Mass transfer occurs as the dispersed phase forms droplets on the plates and moves countercurrently between stages. Engineers can design perforated plate columns using rate equations to model mass transfer and locate a pseudoequilibrium curve, which is then used with an operating line to determine the required number of stages. The design procedure involves iteratively guessing composition values to calculate flow rates and ensure they match at equilibrium.
wholw Content is covered in this presentation .it will give u a basic idea and types about leaching and it will also provide u information via Diagrams .
This document provides an overview of distillation concepts and methods. It discusses general principles of continuous distillation operations and related separation processes. Various thermodynamic models, data correlations, and methods for analyzing distillation columns are presented, including graphical and rigorous computational approaches. Enhanced distillation techniques like azeotropic distillation and extractive distillation are also covered to facilitate separations involving azeotropes or close-boiling components.
Gas absorption is a process used to separate gases by contacting a gas mixture with a liquid solvent. The key principles are the solubility of the absorbed gas and the rate of mass transfer as the gas dissolves into the liquid. Absorption is usually carried out counter-currently in vertical columns. The solvent is fed at the top while the gas enters at the bottom, allowing the absorbed substances to be washed out in the downward flowing liquid. Proper selection of solvent considers factors like gas solubility, volatility, cost, and viscosity. Rate of absorption is determined by volumetric mass transfer coefficients, which can be calculated from operating line and equilibrium curve diagrams.
This document discusses the McCabe Thiele method for calculating multistage separation processes. It provides examples of how to use the method graphically to determine the number of theoretical stages, flow rates, and other parameters. Specifically, it discusses how to: 1) draw equilibrium curves and operating lines to determine minimum reflux ratio and feed location; 2) calculate flow rates, number of stages, and utilities using material balances; and 3) handle special cases like multiple feeds, enriched/stripped sections, and side product specifications. An example problem demonstrates applying these steps to design a binary distillation column with two feed streams.
it is a mass transfer operation use in chemical industries
it is a simple diffusion of solid to liquid phase and foam a new concentrate liquid solution
it is base on simple diffusion how to work in industries this operation
it is use for pharma, seeds and oil industries.
This document summarizes a student project to determine the damping coefficient of SAE20W50 engine oil mixed with activated carbon from coconut shells (biochar). Experiments were conducted using a Universal Vibration Apparatus to measure the damping coefficient of the oil-biochar mixtures and pure SAE20W50 oil. The damping coefficient increased as the percentage of biochar added to the oil increased, with the highest damping observed for a 15% biochar mixture. The results show that adding biochar can improve the damping properties of SAE20W50 engine oil.
Method 8260C by Purge and Trap Gas Chromatography Mass Spectrometry using the...PerkinElmer, Inc.
The document describes a study evaluating the performance of a PerkinElmer Clarus SQ 8 GC/MS using EPA Method 8260C for analyzing volatile organic compounds. Key findings include:
1) The GC/MS system met or exceeded all Method 8260C performance criteria for calibration, detection limits, precision, and accuracy when analyzing 31 volatile organic compounds.
2) Detection limits were as low as 0.05 μg/L and precision and accuracy were within accepted ranges of 76-109% and 0.9-7.4%, respectively.
3) The fast cooling GC oven and high throughput of the system allowed analysis times of under 30 minutes between samples.
The document describes setting up and simulating an atmospheric crude distillation column in HYSYS. It involves characterizing the crude oil feed using assay data, installing a pre-fractionation train with a separator, heater and mixer to determine the feed to the column, and then installing the column along with defining steam and energy streams. The column is configured as a 29 stage ideal column with overhead, bottoms and side product draws using a built-in 3 stripper crude column template.
This document presents a process design for producing ethanol from sugarcane at a plant in Louisiana. It includes mass and energy balances for the four main processes: milling, juice clarification, fermentation, and distillation. The total equipment cost is $21 million and the projected revenue is $145 million per year. A cash flow analysis over 20 years using a 7% discount rate yields a positive net present value of $60 million.
This document provides an overview and details of the raw water pretreatment system for a 6 x 600 MW subcritical coal-fired power plant project in Chhattisgarh, India. The raw water pretreatment system uses coagulation, clarification, and filtration processes to remove suspended solids and colloids from raw water sourced from the Mahanadi river system. Key equipment includes coagulant dosing, mechanically accelerated clarification tanks, and filters. The document also outlines design raw water quality parameters and treatment system capacity.
Optimization of Separator Train in Oil IndustryIRJET Journal
This document discusses optimization of the separator train in the oil industry. It begins with an abstract describing how crude oil extracted from reservoirs is a mixture of oil, gas, water and other impurities. Separators are used to separate these components. The document then provides details on separator tests conducted to determine how the reservoir fluid's volumetric behavior changes as it passes through separators. These tests provide data to optimize separator operating conditions and maximize stock tank oil production. Tables of sample fluid composition and separator test results are included. The objectives of single and multi-stage separator tests are described. Calculations for determining properties like oil formation volume factor, solution gas-oil ratio and stock tank oil gravity are presented using the test data. Overall, the
PRODUCTION OF 60, 000 MTPA OF OLEOCHEMICAL METHYL ESTER FROM RBD PALM KERNEL ...SAJJAD KHUDHUR ABBAS
OBJECTIVES
To produce 60,000 MTPA of methyl esters from RBD palm kernel oil.
To achieve the production of methyl esters by using homogeneous base-catalyzed transesterification method with sodium methoxide (NaOCH3) as catalyst.
The document presents a progress report on dynamic modeling of a batch bioreactor for trans-esterification of waste vegetable oil to produce biodiesel. The report summarizes characterization of the waste vegetable oil, preliminary trans-esterification experiments investigating the effects of temperature and impeller position, simulated hydrodynamic effects using computational fluid dynamics, and outlines ongoing and future work including dynamic reaction modeling and validation experiments.
This paper describes two methods for predicting crankshaft loading and bearing performance in engines: the statically determinate method and the statically indeterminate method. The determinate method assumes the crankshaft is rigid and reaction forces depend only on adjacent loads, while the indeterminate method uses finite element analysis to model crankshaft flexibility and accounts for influences of all loads. Results show the indeterminate method predicts up to 44% higher oil film pressures and loads. This allows for more accurate calculation and lighter crankshaft design by analyzing stresses and flexibility effects.
Boiler ea case study 16 jan 2012 varanasiD.Pawan Kumar
This document provides a summary of key parameters from a case study on assessing boiler efficiency at a 200 MW power plant in India over 9 trials. It includes the objectives, instruments used, methodology, basis for heat loss calculations, boiler parameters monitored, design operating parameters, and findings from the trials on auxiliary consumption, coal consumption, heat rate, and comparisons to design values. The trials assessed parameters like power generation, coal consumption, flue gas analysis, and found average power generation was around 180 MW with overall heat rates ranging from 248 to 266 kcal/kWh.
Isothermal Methanol Converter (IMC) UA Distribution AnalysisGerard B. Hawkins
Isothermal Methanol Converter (IMC) UA Distribution Analysis - Case Study: #0630416GB/H; ACME Co. 9,000 MTD MeOH
This converter uses plates instead of tubes to remove the heat from the reaction gas. The use of the plates and the orientation allow the heat transfer within the converter to be more accurately controlled to follow the maximum rate line.
This case study examines the Radial Flow – Isothermal Methanol Converter (IMC) for ACME Co. 9,000 MTD, based on the Casale Isothermal Methanol Converter (IMC) design.
This document discusses options for distilling dilute ethanol to produce 99.5% ethanol. It analyzes pressure swing distillation versus azeotropic distillation, with benzene as a common entrainer. Preliminary simulations show pressure swing distillation yields the desired product composition with less ethanol loss. A three-column system is also considered but deemed too costly. The document outlines objectives of determining the optimal distillation method, finalizing a process flow diagram, performing safety and economic analyses, and achieving a 5% annual ROI.
The document describes a study that used dissolved air flotation (DAF) to treat wastewater from an oil refinery in Kermanshah, Iran. Experiments were conducted to examine the effect of flow rate, saturation pressure, and coagulant dosage on chemical oxygen demand (COD) removal efficiency. Response surface methodology (RSM) was then used to model COD removal and optimize the DAF process conditions. The maximum predicted COD removal of 67.87% was achieved at specific ranges for flow rate, saturation pressure, and coagulant dosage according to the RSM model.
Determination of Argon in Ammonia Plant Process Gas Streams by Gas Chromatogr...Gerard B. Hawkins
Determination of Argon in Ammonia Plant Process Gas Streams by Gas Chromatography
SCOPE AND FIELD OF APPLICATION
This document is a method for the determination of argon in process gas streams in the range 0-10% v/v.
This document summarizes an experiment comparing droplet breakup using a batch system versus a continuous system with an in-line rotor-stator mixer. The experiment varied the rotor speed from 3000 to 9000 RPM and pump flow rate from 333 to 999 to analyze how these factors impacted droplet size using a Mastersizer 3000. Equations were developed to predict optimum droplet size for each system based on rotor speed and flow rate. While both systems were viable, the continuous system had lower capital costs and easier quality control. Further experiments varying oil viscosity and fraction were recommended.
Advanced Numerical Methods for Modeling Oil-Recovery Processes using Pore- to...Anastasia Dollari
The document discusses various techniques for oil recovery from reservoirs, including primary, secondary, and tertiary (enhanced oil recovery - EOR) methods. It focuses on waterflooding as the most widely used secondary recovery method, where water is injected into the reservoir to displace oil towards producing wells. On average, primary production recovers 15-25% of original oil in place (OOIP), secondary recovery such as waterflooding recovers 20-40% of OOIP, and EOR can recover an additional 5-15% of OOIP, bringing total recovery to 45-60% of OOIP in mature fields. The efficiency of recovery depends on microscopic fluid distribution and displacement at the pore-scale.
Design and implementation of a control structure for quality products in a cr...ISA Interchange
In recent years, interest for petrochemical processes has been increasing, especially in refinement area. However, the high variability in the dynamic characteristics present in the atmospheric distillation column poses a challenge to obtain quality products. To improve distillates quality in spite of the changes in the input crude oil composition, this paper details a new design of a control strategy in a conventional crude oil distillation plant defined using formal interaction analysis tools. The process dynamic and its control are simulated on Aspen HYSYS dynamic environment under real operating conditions. The simulation results are compared against a typical control strategy commonly used in crude oil atmospheric distillation columns.
Recycling and Re-utilization of Steel Plant Waste by using DOEYASH DALAL
The document discusses utilizing steel plant waste through optimizing binder proportions using design of experiments (DOE). Three steel plant waste samples were collected and analyzed. A 2x3 orthogonal array experiment was conducted varying starch and molasses binder levels. Results showed the combination of 2.5% starch and 5% molasses provided the maximum strength of 1196.82 N/pellet and minimum shatter index of 0.18. A 3x3 orthogonal array experiment is being conducted varying binder levels and raw material composition to further optimize pellet properties.
The document discusses the benefits of standby time in adsorption dehydration processes. It describes how molecular sieves are used to dehydrate natural gas and how their capacity declines over cycles due to loss of structure. Having excess regeneration capacity, or standby time, allows operators to reduce cycle times and extend the life of molecular sieves. The document presents a case study where performance testing revealed capacity would decline faster than designed. Using standby time by reducing cycle times allowed the unit to operate for longer than the planned 3 years before recharge.
Similar to Chemical Design of Extraction Column (20)
Electric vehicle and photovoltaic advanced roles in enhancing the financial p...IJECEIAES
Climate change's impact on the planet forced the United Nations and governments to promote green energies and electric transportation. The deployments of photovoltaic (PV) and electric vehicle (EV) systems gained stronger momentum due to their numerous advantages over fossil fuel types. The advantages go beyond sustainability to reach financial support and stability. The work in this paper introduces the hybrid system between PV and EV to support industrial and commercial plants. This paper covers the theoretical framework of the proposed hybrid system including the required equation to complete the cost analysis when PV and EV are present. In addition, the proposed design diagram which sets the priorities and requirements of the system is presented. The proposed approach allows setup to advance their power stability, especially during power outages. The presented information supports researchers and plant owners to complete the necessary analysis while promoting the deployment of clean energy. The result of a case study that represents a dairy milk farmer supports the theoretical works and highlights its advanced benefits to existing plants. The short return on investment of the proposed approach supports the paper's novelty approach for the sustainable electrical system. In addition, the proposed system allows for an isolated power setup without the need for a transmission line which enhances the safety of the electrical network
Understanding Inductive Bias in Machine LearningSUTEJAS
This presentation explores the concept of inductive bias in machine learning. It explains how algorithms come with built-in assumptions and preferences that guide the learning process. You'll learn about the different types of inductive bias and how they can impact the performance and generalizability of machine learning models.
The presentation also covers the positive and negative aspects of inductive bias, along with strategies for mitigating potential drawbacks. We'll explore examples of how bias manifests in algorithms like neural networks and decision trees.
By understanding inductive bias, you can gain valuable insights into how machine learning models work and make informed decisions when building and deploying them.
Literature Review Basics and Understanding Reference Management.pptxDr Ramhari Poudyal
Three-day training on academic research focuses on analytical tools at United Technical College, supported by the University Grant Commission, Nepal. 24-26 May 2024
ACEP Magazine edition 4th launched on 05.06.2024Rahul
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Chemical Design of Extraction Column
1. i
CONTENTS
LIST OF TABLES..................................................................................................ii
LIST OF FIGURES...............................................................................................iii
LIST OF ABBREVIATION ....................................................................................iv
CHAPTER 3 LIQUID LIQUID EXTRACTION COLUMN.....................................3-6
3.1 Liquid Liquid Extraction Column, T-102 ...................................................3-6
3.2 Extraction Unit Selection..........................................................................3-6
3.3 Chemical Design of Karr Reciprocating-Plate Extractor, T-102................3-8
3.3.1 Karr Reciprocating-Plate Extractor Designing Method ....................3-8
3.3.2 Summary of Flow Rate and Composition each Stream ...................3-9
3.3.3 Selection of Key Component......................................................... 3-10
3.3.4 Sizing of a Karr Reciprocating-Plate Extractor .............................. 3-10
2. ii
LIST OF TABLES
Table 3.1: Feed Stream Flow Rate and Composition........................................3-9
Table 3.2: Extract Stream Flow Rate and Composition.....................................3-9
Table 3.3: Raffinate Stream Flow Rate and Composition................................ 3-10
Table 3.4: Solvent Stream Flow Rate and Composition .................................. 3-10
Table 3.5: Minimum HETS and Volumetric Efficiency for the Karr, Reciprocating-
Plate Extractor............................................................................................................ 3-16
3. iii
LIST OF FIGURES
Figure 3.1: Decision guide for extractor selection .............................................3-7
Figure 3.2: The Karr Reciprocating-Plate Extractor...........................................3-8
4. iv
LIST OF ABBREVIATION
WCO Waste cooking oil
FAME Fatty acid methyl ester
TG Triglycerol
FFA Free fatty acid
MeOH Methanol
6. 3-6
CHAPTER 3
LIQUID LIQUID EXTRACTION COLUMN
3.1 Liquid Liquid Extraction Column, T-102
Liquid liquid extraction is one of the common method used in industries. Basically,
liquid liquid extraction is the separation of the components of a liquid mixture by treatment
which one or more of the desired components is preferentially soluble. In this process, it
is essential that the liquid-mixture feed and solvent are at least partially if not completely
immiscible. Fundamentally, three stages are involved. First is to bring the feed mixture and
the solvent into intimate contact resulting the separation of the two phases. Then the
solvent from each phase will be removed and recovered (R.K Sinnot).
Liquid-liquid extraction is an important unit operation and finds applications in
industries such as refinery, pharmaceutical industries, metallurgical industries and other
industries. In biofuel industry, the purity level of biodiesel has strong effect on fuel
properties, engine performance and engine life. Therefore, a purification step is necessary.
In biodiesel production plant, water washing method is used in order to purify biodiesel.
The main purpose of water washing is to separate FAME from the glycerol, methanol and
catalyst. This process also can remove other contaminant in the system that might interfere
with the next step of producing high purity level of biodiesel [1].
3.2 Extraction Unit Selection
The selection of extractor type depends upon many factors including the required
number of theoretical stages or transfer units, required production rate, tolerance to
fouling, ease of cleaning, availability of the required materials of construction, as well as
the ability to handle high or low interfacial tension, high or low density difference, and high
or low viscosities. Figure 3.1 below shows simplified guidance flowchart for selection of
extractor.
7. 3-7
Figure 3.1: Decision guide for extractor selection
Hence, from the guidance flowchart above, reciprocating plate column type of
extractor has been chosen for the water washing process. Since the water washing in
biodiesel production is a process that will cause the formation of emulsion, Karr
Reciprocating Plate Extractor which is a descendent of reciprocating plate column will be
used. This is because Karr Reciprocating Plate Extractor is an extractor that is well suited
with mixtures with emulsifying tendency [2]. Emulsion formation is caused by the reaction
of unreacted waste cooking oil and soap with water. Figure 3.2 below shows the Karr
Reciprocating Plate Column with its main components.
8. 3-8
Figure 3.2: The Karr Reciprocating-Plate Extractor
3.3 Chemical Design of Karr Reciprocating-Plate Extractor, T-102
3.3.1 Karr Reciprocating-Plate Extractor Designing Method
1) Determination of mass fraction of key component
2) Calculate the maximum slope of operating line of the system.
3) Determination of the feed mass flow rate to the solvent mass flow rate, sf mm ,
and the operating solvent flow rate, sm .
4) Calculate the mass fraction of key component in the entering light phase, ky1 , in
the light phase.
5) Determine the extraction factor, EA .
6) Calculate the number of equilibrium stages, eN by using the Kremser-Souders-
Brown theoretical stage equation.
7) Calculate the cross sectional area, A , by dividing by the total volumetric flow rate
(the sum of the volumetric flow rates for both phases) by the total volumetric flow
9. 3-9
rate per unit of extractor cross-sectional area, obtained from the Minimum NETS
and Volumetric Efficiency for the Karr, Reciprocating-Plate Extractor table.
8) Hence, the diameter, D , can be calculated.
9) Find height equivalent tower stages (HETS), at 1D by obtaining required data from
the Effect of Interfacial Tension on HETS for RDC and RPC Extractors table.
10) Calculate the extractor height, Z .
3.3.2 Summary of Flow Rate and Composition each Stream
The data of mass flow rate is obtained from Aspen simulation, hence the molar flow
rate, mole fraction and mass fraction of each stream is calculated and tabulated in tables
below.
Table 3.1: Feed Stream Flow Rate and Composition
Component Flow rate
( hkg / )
Molar flow rate
( hkmol / )
Mole fraction Mass Fraction
Methanol 529.968 16.54081 0.60 0.15
FAME 2292.05 7.730494 0.28 0.66
Glycerol 237.31 2.576831 0.09 0.069
Sulphuric Acid 29.006 0.295746 0.01 0.008
Triacylglycerol 374.69 0.423169 0.015 0.11
Table 3.2: Extract Stream Flow Rate and Composition
Component Flow rate
( hkg / )
Molar flow rate
( hkmol / )
Mole fraction Mass Fraction
Methanol 529.968 16.54081 0.16 0.56
FAME - - - -
Glycerol 237.31 2.576831 0.01 0.25
Sulphuric Acid 29.006 0.295746 0.002 0.03
Water 153.3645 153.3645 0.89 0.16
10. 3-10
Table 3.3: Raffinate Stream Flow Rate and Composition
Component Flow rate
( hkg / )
Molar flow rate
( hkmol / )
Mole fraction Mass Fraction
Methanol - - - -
FAME 2292.05 7.730493 0.88 0.856
Glycerol - - - -
Triacylglycerol 374.687 0.42317 0.05 0.14
Water 12.178 0.675997 0.07 0.004
Solvent Stream
Table 3.4: Solvent Stream Flow Rate and Composition
Component Flow rate
( hkg / )
Molar flow rate
( hkmol / )
Mole fraction Mass Fraction
Water 2775.08 154.0404 1 1
3.3.3 Selection of Key Component
In biodiesel water washing liquid liquid extraction system, to design the Karr
Reciprocating Plate Extractor, methanol will be selected as the key component. This is
due to its solubility of methanol in both feed and solvent stream. Methanol (solute) also
has higher affinity towards the solvent which is water. Hence, making it easier to separate
methanol from FAME. Even though, glycerol is also soluble and miscible with both water
and FAME, glycerol is not selected as the key component as the amount is too small
compared to methanol.
3.3.4 Sizing of a Karr Reciprocating-Plate Extractor
To size the reactor, method or procedure above will be followed. Because FAME
is lighter than the solvent, water, it is introduced at the bottom and water at the top of the
extractor. Data such as flow rate and mass fraction of each stream are obtained from the
mass fraction and mole fraction.
11. 3-11
Feed Composition Data:
Methanol : 529.968 kg/h (0.15 mass fraction)
FAME : 2292.05 kg/h (0.66 mass fraction)
Glycerol : 237.31 kg/h (0.069 mass fraction)
Sulphuric Acid : 20.006 kg/h (0.008 mass fraction)
Triacylglycerol : 374.69 kg/h (0.11mass fraction)
Total flow rate : 3454.024 kg/h
3.3.4.1 Methanol Recovery
= 99%
Based on the data obtained by Aspen simulation, the methanol recovery, , should
be 100%, but it is impossible to have 100% of methanol recovery, hence, 99% of methanol
recovery value will be used in the calculation.
3.3.4.2 Methanol Distribution Coefficient
K = 2.0
Distribution coefficient is a the ratio of concentrations of a compound in a mixture
of two immiscible phases at equilibrium. The value of methanol distribution is estimated by
Drew et. Al [3].
3.3.4.3 Continuous Phase Flux
C = 0.5 gal/min-ft2
Karr Reciprocating Plate Extractor is one type of pulsed-column extractor, where
for pulsed-column extractor, a continuous-phase flux coefficient value of 0.5 is used [4].
3.3.4.4 Mass Fraction of Key Component (Methanol) in the Raffinate
In order to determine the calculated value of methanol in the raffinate, the mass
balance equation will be used
12. 3-12
kk xx 12 )1(
Where
kx2 = Mass fraction of methanol in raffinate
= Methanol recovery
kx1 = Mass fraction of methanol in feed
15.0)99.01(2 kx
0015.02 kx
3.3.4.5 Operating Feed to Minimum Solvent Flow Rate Ratio
kk
kkk
SM
f
xx
yxK
m
m
21
21
Where
fm = Operating feed flow rate, hkg /
SMm = Minimum solvent flow rate, hkg /
K = Methanol distribution coefficient
ky2 = Mass fraction of methanol at solvent stream
0015.015.0
0)15.0(0.2
SM
f
m
m
02.2
SM
f
m
m
3.3.4.6 Minimum Solvent Flow Rate, kg/h
The minimum solvent flow rate can be calculated by using the operating feed flow
rate to minimum solvent flow rate ratio.
02.2
SM
f
m
m
13. 3-13
fm = total operating feed flow rate = 3454.024 kg/h
Hence,
02.2
f
SM
m
m
02.2
/024.3454 hkg
mSM
hkgmSM /913.1709
The minimum amount of water flow rate at the solvent stream is 1709.913 kg/h
3.3.4.7 Operating Solvent Flow Rate, kg/h
SM
f
S
f
m
m
C
m
m
)02.2(5.0
/024.3454
Sm
hkg
hkgmS /826.3419
3.3.4.8 Mass Fraction of Methanol at the Extract Stream, ky1
To obtain the mass fraction of methanol at extract, substitute 0015.02 kx , which
is the mass fraction of methanol in the raffinate stream, and 01.1/ Sf mm into the
equation below:
)( 2121 kk
s
f
kk xx
m
m
yy
)0015.015.0(01.101 ky
15.01 ky
14. 3-14
3.3.4.9 Extraction Factor, AE
Extraction factor is a measure of the ability of the system to separate between two
or more components in a liquid mixture. Extraction factor can be calculated by using the
equation below:
k
S
f
E
K
m
m
A
Where
AE = Extraction factor
fm = Operating feed flow rate, hkg /
sm = Operating solvent flow rate, hkg /
K = Methanol distribution coefficient
2
01.1
EA
505.0EA
3.3.4.10 Number of Equilibrium Stages, NE
It is assumed that, in the system, the solutions are dilute so that the operating and
equilibrium curves are linear. Thus, the Kremser-Souders-Brown Equilibrium Stage
Equation, can be used to calculate the number of equilibrium stages [2].
E
EE
kk
kk
E
A
AA
Kyx
Kyx
N
1
log
)1(
)/(
)/(
log
22
21
Where,
NE = Number of equilibrium stages
kx2 = Mass fraction of methanol in raffinate
kx1 = Mass fraction of methanol in feed
K = Methanol distribution coefficient
15. 3-15
AE = Extraction factor
505.0
1
log
505.0)505.01(
00015.0
015.0
log
EN
73.5EN Equilibrium stages 6 equilibrium stages
3.3.4.11 Determination of Height Equivalent Tower Stage, HETS
HETS is co-related with the interfacial tension of components in a mixture. The
common method to determine HETS is by using the Effect of Interfacial Tension on HETS
for the RDC and RPC Extractors table. However, the interfacial tension data of the
components in this process does not appear to be available.
To solve this problem, Karr et. al, comes out with an alternative method to find
HETS where the HETS for an extractor can be estimated by using scaling rule developed
by them and the experimental values of HETS was summarized in the Minimum HETS
and Volumetric Efficiency for the Karr Reciprocating-Plate Extractor table [5]. Before that,
we must determine whether the extraction system is low interfacial tension system (MIBK,
acetic acid, water system) or high interfacial tension system (o-xylene, acetic acid, water
system).
According to Binks et. al, the extraction system of biodiesel purification (water washing)
process is a low interfacial tension system. This can be proved by the formation of
emulsion in the system [6]. Emulsification is one of the indication that the extraction system
is low interfacial tension system.
16. 3-16
Table 3.5: Minimum HETS and Volumetric Efficiency for the Karr, Reciprocating-Plate Extractor
From the table above, extractor with 12 inches (0.305 m) diameter which is
estimated to be close to the calculated diameter is selected. Then, the solvent or
extractant of the extraction system must be determine in order to choose the right
combination of extractant and dispersed phase. In water washing extraction system, the
solvent (water) is dispersed at the top of the extractor, (take note that in MIBK-Acetic acid-
Water system, when water is selected as solvent, water will be dispersed at the top of the
extractor because the density is higher than MIBK). Hence, this will narrow down the
choice of extractor into only 3 which is in the blue box. Then, between these three, choose
the extractor that give the maximum volumetric efficiency (red box).
After deciding the extractor from the table, minimum HETS and the total volumetric
throughput can be determined.
Minimum HETS = 11.05 stages
17. 3-17
Total Volumetric Throughput = 1694 gal/(h)(ft2
) or 69.023 m3
/(m2
)(h)
3.3.4.12 Cross-sectional Area of Extractor’s Column
In order to calculate the column cross-sectional area, volumetric flow rate of both
inlet streams is required.
Feed stream volumetric flow rate =
f
fm
fm = Operating feed flow rate, hkg /
f = Density of component at feed stream
Sm = Operating feed flow rate, hkg /
S = Density of component at feed stream
Feed stream volumetric flow rate:
33333
/875
/69.374
/1840
/006.29
/1260
/31.237
/9.873
/05.2292
/792
/968.529
mkg
hkg
mkg
hkg
mkg
hkg
mkg
hkg
mkg
hkg
kgm /92.3 3
Solvent stream volumetric flow rate:
3
/1000
/826.3419
mkg
hkg
hm /42.3 3
Then, substitute the value of volumetric flow rate obtained into the equation below
to obtain the cross-sectional area of the extractor’s column
T
SSff
J
mm
A
)]/()/[(
A = Cross-sectional area of extractors column
TJ = Total volumetric flow rate per unit area
hmm
hm
A 23
3
/023.69
]/)42.392.3[(
18. 3-18
2
106.0 mA
3.3.4.13 Extraction Column’s Diameter
Substitute the value of cross-sectional area of the extractor’s column into the
equation below to obtain the diameter of the column.
4
2
D
A
2/12
)106.0(4
m
D
mD 367.0 or inches45.14
3.3.4.14 Karr Reciprocating-Plate Extractor Scale Up
In order to maximize the production of biodiesel and also to increase the level of
purity of biodiesel, Karr Reciprocating-Plate Extractor must be scaled up from pilot to
commercial scale. Equation below is used for this step:
38.0
D
D
HETS
HETS CC
Where,
CHETS = Height equivalent tower stages at commercial scale
HETS = Height equivalent tower stages at pilot scale
Because D obtained is less than 30 inches or 0.762m, standard pipe size which is
the Schedule 10S pipe will be used. Schedule 10S pipe has an inside diameter of 10.42
inches and the most common used pipe for extraction unit system. Hence, the scaling up
calculation can be proceeded.
38.0
12
42.10
05.11
CHETS
inchesHETSC 473.10 , m266.0
20% increment is done to prevent flooding at the extractor’s column. Therefore, the design
of HETSc after 20% increment is 12.567 inches [5].
19. 3-19
3.3.4.15 Extractor Height
After obtaining the HETSC, the height of the extractor can be calculated by using
equation below
DHETSNZ CEE )(
45.14)567.12(6 EZ
inchesZE 85.89 or m28.2
3.3.4.16 Top and Bottom Settler Diameter and Height
Finally is to add top and bottom sections which will act as settlers to separate the
phases. The diameter of both settlers is 50% greater than the extractor diameter and the
height of each settler is equal to the settler diameter [7].
Diameter of both settlers is:
)42.10(5.1 inchesDS
inchesDS 63.15 or m397.0
Therefore, the total height for both settlers is:
inchesZS 26.31)42.10)(5.1(2 or m794.0
3.3.4.17 Total Height of Karr Reciprocating-Plate Extractor Tower
SE ZZZ
inchesZ )26.3185.89(
inchesZ 11.121 or m076.3
20. 3-20
REFERENCES
[1] Shuchen B Thakore and Bharat I Bhatt, Introduction to Process Engineering and
Design, Second. New Delhi: Mc Graw Hill, 2015.
[2] John W. green & Robert H. Perry, Perry’s Chemical Engineers Handbook. 2008.
[3] J. . Drew, “Design for Solvent Recovery,” Chem. Eng. J., vol. 2, 1975.
[4] J. . Valle-Riesta, “Project Evaluation in The Chemical Process Industries,” Proj.
Eval. Chem. Process Ind., 1983.
[5] T. C. Karr, A., Lo, “Scale-up of Large Diameter Reciprocating-Plate Extraction
Column,” Chem. Eng. Progr., no. 72, p. 11, 1976.
[6] B. P. Binks, P. D. I. Fletcher, and D. N. Petsev, “Tension System,” no. 9, pp. 1025–
1034, 2000.
[7] H. Silla, Design and Economics. 2003.