FULL COURSE:
https://courses.chemicalengineeringguy.com/p/flash-distillation-in-chemical-process-engineering/
Introduction:
Binary Distillation is one of the most important Mass Transfer Operations used extensively in the Chemical industry.
Understanding the concept behind Gas-Gas, Liquid-Liquid and the Gas-Liquid mass transfer interaction will allow you to understand and model Distillation Columns, Flashes, Batch Distillator, Tray Columns and Packed column, etc...
We will cover:
REVIEW: Of Mass Transfer Basics (Equilibrium VLE Diagrams, Volatility, Raoult's Law, Azeotropes, etc..)
Distillation Theory - Concepts and Principles
Application of Distillation in the Industry
Equipment for Flashing Systems such as Flash Drums
Design & Operation of Flash Drums
Material and Energy Balances for flash systems
Adiabatic and Isothermal Operation
Animations and Software Simulation for Flash Distillation Systems (ASPEN PLUS/HYSYS)
Theory + Solved Problem Approach:
All theory is taught and backed with exercises, solved problems, and proposed problems for homework/individual study.
At the end of the course:
You will be able to understand mass transfer mechanism and processes behind Flash Distillation.
You will be able to continue with Batch Distillation, Fractional Distillation, Continuous Distillation and further courses such as Multi-Component Distillation, Reactive Distillation and Azeotropic Distillation.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating.
There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
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.
FULL COURSE:
https://courses.chemicalengineeringguy.com/p/flash-distillation-in-chemical-process-engineering/
Introduction:
Binary Distillation is one of the most important Mass Transfer Operations used extensively in the Chemical industry.
Understanding the concept behind Gas-Gas, Liquid-Liquid and the Gas-Liquid mass transfer interaction will allow you to understand and model Distillation Columns, Flashes, Batch Distillator, Tray Columns and Packed column, etc...
We will cover:
REVIEW: Of Mass Transfer Basics (Equilibrium VLE Diagrams, Volatility, Raoult's Law, Azeotropes, etc..)
Distillation Theory - Concepts and Principles
Application of Distillation in the Industry
Equipment for Flashing Systems such as Flash Drums
Design & Operation of Flash Drums
Material and Energy Balances for flash systems
Adiabatic and Isothermal Operation
Animations and Software Simulation for Flash Distillation Systems (ASPEN PLUS/HYSYS)
Theory + Solved Problem Approach:
All theory is taught and backed with exercises, solved problems, and proposed problems for homework/individual study.
At the end of the course:
You will be able to understand mass transfer mechanism and processes behind Flash Distillation.
You will be able to continue with Batch Distillation, Fractional Distillation, Continuous Distillation and further courses such as Multi-Component Distillation, Reactive Distillation and Azeotropic Distillation.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating.
There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
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.
FULL COURSE:
https://courses.chemicalengineeringguy.com/p/flash-distillation-in-chemical-process-engineering/
Introduction:
Binary Distillation is one of the most important Mass Transfer Operations used extensively in the Chemical industry.
Understanding the concept behind Gas-Gas, Liquid-Liquid and the Gas-Liquid mass transfer interaction will allow you to understand and model Distillation Columns, Flashes, Batch Distillator, Tray Columns and Packed column, etc...
We will cover:
REVIEW: Of Mass Transfer Basics (Equilibrium VLE Diagrams, Volatility, Raoult's Law, Azeotropes, etc..)
Distillation Theory - Concepts and Principles
Application of Distillation in the Industry
Equipment for Flashing Systems such as Flash Drums
Design & Operation of Flash Drums
Material and Energy Balances for flash systems
Adiabatic and Isothermal Operation
Animations and Software Simulation for Flash Distillation Systems (ASPEN PLUS/HYSYS)
Theory + Solved Problem Approach:
All theory is taught and backed with exercises, solved problems, and proposed problems for homework/individual study.
At the end of the course:
You will be able to understand mass transfer mechanism and processes behind Flash Distillation.
You will be able to continue with Batch Distillation, Fractional Distillation, Continuous Distillation and further courses such as Multi-Component Distillation, Reactive Distillation and Azeotropic Distillation.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating.
There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
Engineers often use softwares to perform gas compressor calculations to estimate compressor duty, temperatures, adiabatic & polytropic efficiencies, driver & cooler duty. In the following exercise, gas compressor calculations for a pipeline composition are shown as an example case study.
A 10-minute experimental run shows that 75% of liquid reactant is converted to product by a half-order rate. What would be the fraction converted in a half-hour run?
Processing of petroleum types of refluxKarnav Rana
PROCESSING OF PETROLEUM :TYPES OF REFLUX
arrangements of distillation towers
Pump back reflux and pump around reflux
Side stripping columns
process refining & petrochemicals
Reactor and Catalyst Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 CATALYST DESIGN
4.1 Equivalent Pellet Diameter
4.2 Voidage
4.3 Pellet Density
5 REACTOR DESIGN
6 CATALYST SUPPORT
6.1 Choice of Support
TABLES
1 CATALYST SUPPORT SHAPES
2 SECONDARY REFORMER SPREADSHEET
FIGURES
1 GRAPH OF EFFECTIVENESS v THIELE MODULUS
2 VARIATION OF COSTS WITH CATALYST SIZE
3 VARIATION OF COSTS WITH CATALYST BED VOIDAGE
4 VARIATION OF COSTS WITH VESSEL DIAMETER
Estimation of Pressure Drop in Pipe Systems
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
3.1 units
4 SOURCES OF DATA
5 BASIC CONCEPTS
5.1 Equation for Pressure Change in a Flowing
Fluid
5.2 Static and Stagnation Pressures
5.3 Sonic Flow
6 INCOMPRESSIBLE FLOW IN PIPES OF CONSTANT
CROSS-SECTION
6.1 Straight Circular Pipes
6.2 Ducts of Non-circular Cross-section
6.3 Coils
6.4 General Equation for Incompressible Flow
in Pipes of Constant Cross-section
7 COMPRESSIBLE FLOW IN PIPES OF CONSTANT
CROSS-SECTION
7.1 Isothermal Flow
7.2 Adiabatic Flow
7.3 Estimation of Pressure Drop for Adiabatic
Flow in Pipes of Constant Cross-section
7.4 Ratio of Isothermal to Adiabatic Pressure Drop
8 FLOW IN PIPE FITTINGS
8.1 Incompressible Flow
8.2 Compressible Flow
9 FLOW IN BENDS
9.1 Incompressible Flow in Bends
9.2 Compressible Flow in Bends
10 CHANGES IN CROSS-SECTIONAL AREA
9.1 Incompressible Flow
9.2 Compressible Flow
11 ORIFICES, NOZZLES AND VENTURIS
11.1 Incompressible Flow through an Orifice
11.2 Compressible Flow through an Orifice or Nozzle
11.3 Venturi Choke Tubes
12 VALVES
12.1 General
12.2 Incompressible Flow in Valves
12.2 Compressible Flow in Valves
13 COMBINING AND DIVIDING FLOW
9.1 Incompressible Flow
9.2 Compressible Flow
14 COMPUTER PROGRAMS FOR FLUID FLOW
15 NOMENCLATURE
16 REFERENCES
APPENDICES
A BASIC THERMODYNAMICS
B COMPRESSIBLE FLOW THROUGH ORIFICES
C THE ‘TWO-K’ METHOD FOR FITTING PRESSURE LOSS
Shortcut Methods of Distillation Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 ESTIMATIONOF PLATEAGE AND REFLUX
REQUIREMENTS
2.1 Generalized Procedure for Nmin and Rmin
2.2 Equation based Procedure for Nmin and Rmin
3 PREDICTION OF OVERALL PLATE EFFICIENCY
4 SIZING OF MAIN PLANT ITEMS
4.1 Column Diameter
4.2 Surface Area of Condensers and Reboilers
FIGURES
1 NON-IDEAL EQUILIBRIUM CURVE
2 AT A GLANCE CHART BASED ON FENSKE,
UNDERWOOD
3 PLATE EFFICIENCY CORRELATION OF O’CONNEL
The Principles required to understand Distillation, Absorption, Stripping, Flashing, Gas Treating, Scrubbing and more!
Introduction:
This course covers all the theory required to understand the basic principles behind Unit Operations that are based on Mass Transfer. Most of these Unit Operations (Equipments) are used in Process Separation Technologies in the Industry.Common examples are Distillation, Absorption and Scrubbing.
This course is required for the following:
Flash Distillation
Gas Absorption & Stripping
Simple Distillation
Batch Distillation
Binary Distillation
Fractional Distillation
Scrubbers
Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers
Tray Towers
We will cover:
Mass Transfer Basics
Diffusion, Convection
Flux & Fick's Law
The Concept of Equilibrium & Phases
Gibbs Phase Rule
Vapor Pressure
Equilibrium Vapor-Liquid Diagrams (T-xy, P-xy, XY)
Equilibrium Curves
Dew Point, Bubble Point
Volatility (Absolute & Relative)
K-Values
Ideal Cases vs. Real Cases
Henry's Law
Raoult's Law
Deviations of Ideal Cases (Positive and Negative)
Azeotropes
Solubility of Gases in Liquids
Interphase Mass Transfer and its Theories
Two Film Theory
Mass Transfer Coefficients (Overall vs Local)
Getting Vapor-Liquid and Solubility Data
Solved-Problem Approach:
All theory is backed with:
Exercises
Solved problems
Proposed problems
Homework
Case Studies
Individual Study
At the end of the course:
You will be able to understand the mass transfer concepts behind various Unit Operations involving Vapor - Liquid Interaction.
You will be able to apply this theory in further Unit Operations related to Mass Transfer Vapor - Liquid, which is one of the most common interactions found in the industry.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating. There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
Engineers often use softwares to perform gas compressor calculations to estimate compressor duty, temperatures, adiabatic & polytropic efficiencies, driver & cooler duty. In the following exercise, gas compressor calculations for a pipeline composition are shown as an example case study.
A 10-minute experimental run shows that 75% of liquid reactant is converted to product by a half-order rate. What would be the fraction converted in a half-hour run?
Processing of petroleum types of refluxKarnav Rana
PROCESSING OF PETROLEUM :TYPES OF REFLUX
arrangements of distillation towers
Pump back reflux and pump around reflux
Side stripping columns
process refining & petrochemicals
Reactor and Catalyst Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
4 CATALYST DESIGN
4.1 Equivalent Pellet Diameter
4.2 Voidage
4.3 Pellet Density
5 REACTOR DESIGN
6 CATALYST SUPPORT
6.1 Choice of Support
TABLES
1 CATALYST SUPPORT SHAPES
2 SECONDARY REFORMER SPREADSHEET
FIGURES
1 GRAPH OF EFFECTIVENESS v THIELE MODULUS
2 VARIATION OF COSTS WITH CATALYST SIZE
3 VARIATION OF COSTS WITH CATALYST BED VOIDAGE
4 VARIATION OF COSTS WITH VESSEL DIAMETER
Estimation of Pressure Drop in Pipe Systems
0 INTRODUCTION/PURPOSE
1 SCOPE
2 FIELD OF APPLICATION
3 DEFINITIONS
3.1 units
4 SOURCES OF DATA
5 BASIC CONCEPTS
5.1 Equation for Pressure Change in a Flowing
Fluid
5.2 Static and Stagnation Pressures
5.3 Sonic Flow
6 INCOMPRESSIBLE FLOW IN PIPES OF CONSTANT
CROSS-SECTION
6.1 Straight Circular Pipes
6.2 Ducts of Non-circular Cross-section
6.3 Coils
6.4 General Equation for Incompressible Flow
in Pipes of Constant Cross-section
7 COMPRESSIBLE FLOW IN PIPES OF CONSTANT
CROSS-SECTION
7.1 Isothermal Flow
7.2 Adiabatic Flow
7.3 Estimation of Pressure Drop for Adiabatic
Flow in Pipes of Constant Cross-section
7.4 Ratio of Isothermal to Adiabatic Pressure Drop
8 FLOW IN PIPE FITTINGS
8.1 Incompressible Flow
8.2 Compressible Flow
9 FLOW IN BENDS
9.1 Incompressible Flow in Bends
9.2 Compressible Flow in Bends
10 CHANGES IN CROSS-SECTIONAL AREA
9.1 Incompressible Flow
9.2 Compressible Flow
11 ORIFICES, NOZZLES AND VENTURIS
11.1 Incompressible Flow through an Orifice
11.2 Compressible Flow through an Orifice or Nozzle
11.3 Venturi Choke Tubes
12 VALVES
12.1 General
12.2 Incompressible Flow in Valves
12.2 Compressible Flow in Valves
13 COMBINING AND DIVIDING FLOW
9.1 Incompressible Flow
9.2 Compressible Flow
14 COMPUTER PROGRAMS FOR FLUID FLOW
15 NOMENCLATURE
16 REFERENCES
APPENDICES
A BASIC THERMODYNAMICS
B COMPRESSIBLE FLOW THROUGH ORIFICES
C THE ‘TWO-K’ METHOD FOR FITTING PRESSURE LOSS
Shortcut Methods of Distillation Design
0 INTRODUCTION/PURPOSE
1 SCOPE
2 ESTIMATIONOF PLATEAGE AND REFLUX
REQUIREMENTS
2.1 Generalized Procedure for Nmin and Rmin
2.2 Equation based Procedure for Nmin and Rmin
3 PREDICTION OF OVERALL PLATE EFFICIENCY
4 SIZING OF MAIN PLANT ITEMS
4.1 Column Diameter
4.2 Surface Area of Condensers and Reboilers
FIGURES
1 NON-IDEAL EQUILIBRIUM CURVE
2 AT A GLANCE CHART BASED ON FENSKE,
UNDERWOOD
3 PLATE EFFICIENCY CORRELATION OF O’CONNEL
The Principles required to understand Distillation, Absorption, Stripping, Flashing, Gas Treating, Scrubbing and more!
Introduction:
This course covers all the theory required to understand the basic principles behind Unit Operations that are based on Mass Transfer. Most of these Unit Operations (Equipments) are used in Process Separation Technologies in the Industry.Common examples are Distillation, Absorption and Scrubbing.
This course is required for the following:
Flash Distillation
Gas Absorption & Stripping
Simple Distillation
Batch Distillation
Binary Distillation
Fractional Distillation
Scrubbers
Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers
Tray Towers
We will cover:
Mass Transfer Basics
Diffusion, Convection
Flux & Fick's Law
The Concept of Equilibrium & Phases
Gibbs Phase Rule
Vapor Pressure
Equilibrium Vapor-Liquid Diagrams (T-xy, P-xy, XY)
Equilibrium Curves
Dew Point, Bubble Point
Volatility (Absolute & Relative)
K-Values
Ideal Cases vs. Real Cases
Henry's Law
Raoult's Law
Deviations of Ideal Cases (Positive and Negative)
Azeotropes
Solubility of Gases in Liquids
Interphase Mass Transfer and its Theories
Two Film Theory
Mass Transfer Coefficients (Overall vs Local)
Getting Vapor-Liquid and Solubility Data
Solved-Problem Approach:
All theory is backed with:
Exercises
Solved problems
Proposed problems
Homework
Case Studies
Individual Study
At the end of the course:
You will be able to understand the mass transfer concepts behind various Unit Operations involving Vapor - Liquid Interaction.
You will be able to apply this theory in further Unit Operations related to Mass Transfer Vapor - Liquid, which is one of the most common interactions found in the industry.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating. There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
This is a slideshow / resource / support material of the course.
Get full access (videlectures)
https://www.chemicalengineeringguy.com/courses/aspen-plus-bootcamp-with-12-case-studies/
x-x-x
Requirements
Basic understanding of Plant Design & Operation
Strong Chemical Engineering Fundamentals
Aspen Plus V10 (at least 7.0)
Aspen Plus – Basic Process Modeling (Very Recommended)
Aspen Plus – Intermediate Process Modeling (Somewhat Recommended)
Description
This BOOTCAMP will show you how to model and simulate common industrial Chemical Processes.
It is focused on the “BOOTCAMP” idea, in which you will learn via workshops and case studies, minimizing theory to maximize learning.
You will learn about:
Better Flowsheet manipulation and techniques
Understand Property Method Selection and its effects on simulation results
More than 15 Unit Operations that can be used in any Industry
Model Analysis Tools required for process design
Reporting Relevant Results Plot relevant data
Analysis & Optimization of Chemical Plants
Economic Analysis
Dynamic Simulations
At the end of this Bootcamp, you will be able to model more industrial processes, feel confident when modeling new processes as well as applying what you have learnt to other industries.
I am Dave J. I am a Nuclear Engineering Exam Helper at liveexamhelper.com. I hold a Masters' Degree in Nuclear Physics from, University of Chicago, USA. I have been helping students with their exams for the past 12 years. You can hire me to take your exam in Nuclear Engineering.
Visit liveexamhelper.com or email info@liveexamhelper.com.
You can also call on +1 678 648 4277 for any assistance with the Nuclear Engineering exams.
BC Chemistry 162 Laboratory Manual Experiment 6 Vapor Press.docxrosemaryralphs52525
BC Chemistry 162 Laboratory Manual
Experiment 6: Vapor Pressure of Liquids
- 1 -
Experiment 6: Vapor Pressure of Liquids
Background
Liquids contain molecules that have different kinetic energies (due to different velocities). Some of the
faster liquid molecules have enough kinetic energy to vaporize. At the same time, some of the slower
vapor molecules condense into liquid. In an open container, the rate of vaporization will be greater than
the rate of condensation—hence, the liquid will eventually evaporate. In a sealed flask, however, there
will be a point in which equilibrium is reached between the rate of vaporization and the rate of
condensation. To the eye, it seems that the liquid doesn’t change at equilibrium. But at the microscopic
level a vapor molecule enters the liquid phase for every liquid molecule that enters the gas phase.
The total pressure in the sealed flask is due to the vaporized liquid plus air molecules present in the flask:
Ptotal = Pvapor + Pair (1)
In this experiment, you will investigate the relationship between
the vapor pressure of a liquid and its temperature. Pressure and
temperature data will be collected using a gas pressure sensor and
a temperature probe (Figure 1). Vapor pressures will be
determined by subtracting atmospheric pressure from the total
pressure.
The flask will be placed in water baths of different temperatures to
determine the effect of temperature on vapor pressure. You will
measure the vapor pressure of methanol and ethanol and
determine the enthalpy (heat) of vaporization for each liquid.
Objectives
In this experiment, you will
Investigate the relationship between the vapor pressure of a liquid and its temperature.
Compare the vapor pressure of two different liquids at the same temperature.
Use pressure‐temperature data and the Clausius‐Clapeyron equation to determine the heat of
vaporization for each liquid.
Caution!
The alcohols used in this experiment are flammable and poisonous. Avoid inhaling their vapors. Avoid
contacting them with your skin or clothing. Be sure there are no open flames in the lab during this
experiment. Notify your teacher immediately if an accident occurs.
Procedure
1. Wear goggles! You will work in pairs for this lab, but you may share water baths with your table.
2. Prepare four water baths: 20 to 25°C (use room temperature water), 30 to 35°C, 40 to 45°C, and 50 to
55°C. You should also have some hot water on a hot plate on reserve.
3. Obtain a temperature probe and gas pressure sensor. The sensor comes with a
rubber‐stopper assembly (Figure 2). The stopper has three holes, one of which
is closed. Make sure your tubing and valve are not inserted in the closed hole.
Insert the rubber‐stopper assembly into a 125 mL Erlenmeyer flask.
Important: Twist the stopper into the neck of the flask to ensure a tight
fit.
Figure 1
Figure 2
BC Ch.
Natural Convection Heat Transfer of Viscoelastic Fluids in a Horizontal AnnulusPMOHANSAHU
a detailed discussion of the results in terms of the streamline profiles, isotherm contours, distribution of local Nusselt number, variation of velocity components, etc., is also presented. Finally, from an application standpoint, a simple correlation for the average Nusselt number is presented, which can be used for the interpolation of the present results for the intermediate values of the governing parameters in a new application.
The Principles required to understand Distillation, Absorption, Stripping, Flashing, Gas Treating, Scrubbing and more!
Introduction:
This course covers all the theory required to understand the basic principles behind Unit Operations that are based on Mass Transfer. Most of these Unit Operations (Equipments) are used in Process Separation Technologies in the Industry.Common examples are Distillation, Absorption and Scrubbing.
This course is required for the following:
Flash Distillation
Gas Absorption & Stripping
Simple Distillation
Batch Distillation
Binary Distillation
Fractional Distillation
Scrubbers
Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers
Tray Towers
We will cover:
Mass Transfer Basics
Diffusion, Convection
Flux & Fick's Law
The Concept of Equilibrium & Phases
Gibbs Phase Rule
Vapor Pressure
Equilibrium Vapor-Liquid Diagrams (T-xy, P-xy, XY)
Equilibrium Curves
Dew Point, Bubble Point
Volatility (Absolute & Relative)
K-Values
Ideal Cases vs. Real Cases
Henry's Law
Raoult's Law
Deviations of Ideal Cases (Positive and Negative)
Azeotropes
Solubility of Gases in Liquids
Interphase Mass Transfer and its Theories
Two Film Theory
Mass Transfer Coefficients (Overall vs Local)
Getting Vapor-Liquid and Solubility Data
Solved-Problem Approach:
All theory is backed with:
Exercises
Solved problems
Proposed problems
Homework
Case Studies
Individual Study
At the end of the course:
You will be able to understand the mass transfer concepts behind various Unit Operations involving Vapor - Liquid Interaction.
You will be able to apply this theory in further Unit Operations related to Mass Transfer Vapor - Liquid, which is one of the most common interactions found in the industry.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating. There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
We live in the 21. century, we drive cars, we have the thermal and nuclear power plants and it all started with the work of Carnot, who established the principle of creating work of en engine from the supplied warmth. However, we have also problems with the pollution of our environment and the created warmth from these technical devices
We live in the 21. century, we drive cars, we have the thermal and nuclear power plants and it all started with the work of Carnot, who established the principle of creating work of en engine from the supplied warmth. However, we have also problems with the pollution of our environment and the created warmth from these technical devices.
An Overview to the most common Industrial Mass Transfer Operations & Process Separation Technologies
Course Description
In this course we will cover the most basic processes involved in Mass Transfer Operations. This is an overview of what type of processes, methods and units are used in the industry. This is mostly an introductory course which will allow you to learn, understand and know the approach towards separation processes involving mass transfer phenomena.
It is an excellent course before any Mass Transfer Process or Unit Operation Course such as Distillations, Extractions, Leaching, Membranes, Absorption, etc...
This course is extremely recommended if you will continue with the following:
Flash Distillation, Simple Distillation, Batch Distillation
Gas Absorption, Desorption & Stripping
Binary Distillation, Fractional Distillation
Scrubbers, Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers, Tray Towers
Membranes
Liquid Extraction
Dryers / Humidifiers
Adsorbers
Evaporators/Sublimators
Crystallizers
Centrifugations
And many other Separation Technology!
At the end of the Course:
You will be able to understand the mass transfer operations concepts. You will be able to identify Mass Transfer Unit Operations. You will be also able to ensure the type of method of separation technology used.
You will be able to apply this theory in further Unit Operations.
Theory-Based Course
This is a very theoretical course, some calculations and exercises are present, but overall, expect mostly theoretical concepts.
An Overview to the most common Industrial Mass Transfer Operations & Process Separation Technologies
Course Description
In this course we will cover the most basic processes involved in Mass Transfer Operations. This is an overview of what type of processes, methods and units are used in the industry. This is mostly an introductory course which will allow you to learn, understand and know the approach towards separation processes involving mass transfer phenomena.
It is an excellent course before any Mass Transfer Process or Unit Operation Course such as Distillations, Extractions, Leaching, Membranes, Absorption, etc...
This course is extremely recommended if you will continue with the following:
Flash Distillation, Simple Distillation, Batch Distillation
Gas Absorption, Desorption & Stripping
Binary Distillation, Fractional Distillation
Scrubbers, Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers, Tray Towers
Membranes
Liquid Extraction
Dryers / Humidifiers
Adsorbers
Evaporators/Sublimators
Crystallizers
Centrifugations
And many other Separation Technology!
At the end of the Course:
You will be able to understand the mass transfer operations concepts. You will be able to identify Mass Transfer Unit Operations. You will be also able to ensure the type of method of separation technology used.
You will be able to apply this theory in further Unit Operations.
Theory-Based Course
This is a very theoretical course, some calculations and exercises are present, but overall, expect mostly theoretical concepts.
An Overview to the most common Industrial Mass Transfer Operations & Process Separation Technologies
Course Description
In this course we will cover the most basic processes involved in Mass Transfer Operations. This is an overview of what type of processes, methods and units are used in the industry. This is mostly an introductory course which will allow you to learn, understand and know the approach towards separation processes involving mass transfer phenomena.
It is an excellent course before any Mass Transfer Process or Unit Operation Course such as Distillations, Extractions, Leaching, Membranes, Absorption, etc...
This course is extremely recommended if you will continue with the following:
Flash Distillation, Simple Distillation, Batch Distillation
Gas Absorption, Desorption & Stripping
Binary Distillation, Fractional Distillation
Scrubbers, Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers, Tray Towers
Membranes
Liquid Extraction
Dryers / Humidifiers
Adsorbers
Evaporators/Sublimators
Crystallizers
Centrifugations
And many other Separation Technology!
At the end of the Course:
You will be able to understand the mass transfer operations concepts. You will be able to identify Mass Transfer Unit Operations. You will be also able to ensure the type of method of separation technology used.
You will be able to apply this theory in further Unit Operations.
Theory-Based Course
This is a very theoretical course, some calculations and exercises are present, but overall, expect mostly theoretical concepts.
An Overview to the most common Industrial Mass Transfer Operations & Process Separation Technologies
Course Description
In this course we will cover the most basic processes involved in Mass Transfer Operations. This is an overview of what type of processes, methods and units are used in the industry. This is mostly an introductory course which will allow you to learn, understand and know the approach towards separation processes involving mass transfer phenomena.
It is an excellent course before any Mass Transfer Process or Unit Operation Course such as Distillations, Extractions, Leaching, Membranes, Absorption, etc...
This course is extremely recommended if you will continue with the following:
Flash Distillation, Simple Distillation, Batch Distillation
Gas Absorption, Desorption & Stripping
Binary Distillation, Fractional Distillation
Scrubbers, Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers, Tray Towers
Membranes
Liquid Extraction
Dryers / Humidifiers
Adsorbers
Evaporators/Sublimators
Crystallizers
Centrifugations
And many other Separation Technology!
At the end of the Course:
You will be able to understand the mass transfer operations concepts. You will be able to identify Mass Transfer Unit Operations. You will be also able to ensure the type of method of separation technology used.
You will be able to apply this theory in further Unit Operations.
Theory-Based Course
This is a very theoretical course, some calculations and exercises are present, but overall, expect mostly theoretical concepts.
An Overview to the most common Industrial Mass Transfer Operations & Process Separation Technologies
Course Description
In this course we will cover the most basic processes involved in Mass Transfer Operations. This is an overview of what type of processes, methods and units are used in the industry. This is mostly an introductory course which will allow you to learn, understand and know the approach towards separation processes involving mass transfer phenomena.
It is an excellent course before any Mass Transfer Process or Unit Operation Course such as Distillations, Extractions, Leaching, Membranes, Absorption, etc...
This course is extremely recommended if you will continue with the following:
Flash Distillation, Simple Distillation, Batch Distillation
Gas Absorption, Desorption & Stripping
Binary Distillation, Fractional Distillation
Scrubbers, Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers, Tray Towers
Membranes
Liquid Extraction
Dryers / Humidifiers
Adsorbers
Evaporators/Sublimators
Crystallizers
Centrifugations
And many other Separation Technology!
At the end of the Course:
You will be able to understand the mass transfer operations concepts. You will be able to identify Mass Transfer Unit Operations. You will be also able to ensure the type of method of separation technology used.
You will be able to apply this theory in further Unit Operations.
Theory-Based Course
This is a very theoretical course, some calculations and exercises are present, but overall, expect mostly theoretical concepts.
The Principles required to understand Distillation, Absorption, Stripping, Flashing, Gas Treating, Scrubbing and more!
Introduction:
This course covers all the theory required to understand the basic principles behind Unit Operations that are based on Mass Transfer. Most of these Unit Operations (Equipments) are used in Process Separation Technologies in the Industry.Common examples are Distillation, Absorption and Scrubbing.
This course is required for the following:
Flash Distillation
Gas Absorption & Stripping
Simple Distillation
Batch Distillation
Binary Distillation
Fractional Distillation
Scrubbers
Gas Treating
Sprayers / Spray Towers
Bubble Columns / Sparged Vessels
Agitation Vessels
Packed Towers
Tray Towers
We will cover:
Mass Transfer Basics
Diffusion, Convection
Flux & Fick's Law
The Concept of Equilibrium & Phases
Gibbs Phase Rule
Vapor Pressure
Equilibrium Vapor-Liquid Diagrams (T-xy, P-xy, XY)
Equilibrium Curves
Dew Point, Bubble Point
Volatility (Absolute & Relative)
K-Values
Ideal Cases vs. Real Cases
Henry's Law
Raoult's Law
Deviations of Ideal Cases (Positive and Negative)
Azeotropes
Solubility of Gases in Liquids
Interphase Mass Transfer and its Theories
Two Film Theory
Mass Transfer Coefficients (Overall vs Local)
Getting Vapor-Liquid and Solubility Data
Solved-Problem Approach:
All theory is backed with:
Exercises
Solved problems
Proposed problems
Homework
Case Studies
Individual Study
At the end of the course:
You will be able to understand the mass transfer concepts behind various Unit Operations involving Vapor - Liquid Interaction.
You will be able to apply this theory in further Unit Operations related to Mass Transfer Vapor - Liquid, which is one of the most common interactions found in the industry.
About your instructor:
I majored in Chemical Engineering with a minor in Industrial Engineering back in 2012.
I worked as a Process Design/Operation Engineer in INEOS Koln, mostly on the petrochemical area relating to naphtha treating. There I designed and modeled several processes relating separation of isopentane/pentane mixtures, catalytic reactors and separation processes such as distillation columns, flash separation devices and transportation of tank-trucks of product.
This is course on Plant Simulation will show you how to setup hypothetical compounds, oil assays, blends, and petroleum characterization using the Oil Manager of Aspen HYSYS.
You will learn about:
Hypothetical Compounds (Hypos)
Estimation of hypo compound data
Models via Chemical Structure UNIFAC Component Builder
Basis conversion/cloning of existing components
Input of Petroleum Assay and Crude Oils
Typical Bulk Properties (Molar Weight, Density, Viscosity)
Distillation curves such as TBP (Total Boiling Point)
ASTM (D86, D1160, D86-D1160, D2887)
Chromatography
Light End
Oil Characterization
Using the Petroleum Assay Manager or the Oil Manager
Importing Assays: Existing Database
Creating Assays: Manually / Model
Cutting: Pseudocomponent generation
Blending of crude oils
Installing oils into Aspen HYSYS flowsheets
Getting Results (Plots, Graphs, Tables)
Property and Composition Tables
Distribution Plot (Off Gas, Light Short Run, Naphtha, Kerosene, Light Diesel, Heavy Diesel, Gasoil, Residue)
Oil Properties
Proper
Boiling Point Curves
Viscosity, Density, Molecular Weight Curves
This is helpful for students, teachers, engineers and researchers in the area of R&D, specially those in the Oil and Gas or Petroleum Refining industry.
This is a "workshop-based" course, there is about 25% theory and about 75% work!
At the end of the course you will be able to handle crude oils for your fractionation, refining, petrochemical process simulations!
COURSE LINK:
https://www.chemicalengineeringguy.com/courses/petroleum-refining/
COURSE DESCRIPTION:
The main scope of the course is to create strong basis and fundamentals regarding the processes in the Petroleum Refining. We take a look to the Oil&Gas Industry briefly and continue directly with the Refining Process. We then make a focus in each individual unit operation in the refinery.
Learn about:
* Oil& Gas Industry
* Difference between Petroleum Refining vs. Petrochemical Industry
* Overview of the most important operations and products
* Market insight (supply/demand) as well as (production/consumption)
* Several Petroleum Refineries around the World
Unit Operations & Processes
* Refining and Fractionation
* Atmospheric Distillation Column
* Vacuum Distillation
* Hydrotreating (Hydrogenation)
* Blending
* Reforming
* Isomerization
* Alkylation
* Steam Cracking
* Fluid Catalytic Cracking
* Gas Sweetening (Hydrodesulfurization)
* Coking
Components:
* Fuel Gas / Natural Gas
* Liquified Petroleum Gases (LPG)
* Propane, Butane
* Sulfur / Hydrogen Sulfide
* Gasoline / Automotive Gas Oil
* Naphtha Cuts (Light/Heavy)
* Kerosene
* Diesel
* Gasoil
* Lubricants
* Vacuum Residues
* Asphalt
* Coke
NOTE: This course is focused for Process Simulation
At the end of the course you will feel confident in the Petroleum Refining Industry. You will know the most common Process & Unit Operations as well as their distribution, production and importance in daily life.
----
Please show the love! LIKE, SHARE and SUBSCRIBE!
More likes, sharings, suscribers: MORE VIDEOS!
-----
CONTACT ME
Chemical.Engineering.Guy@Gmail.com
www.ChemicalEngineeringGuy.com
http://facebook.com/Chemical.Engineering.Guy
You speak spanish? Visit my spanish channel -www.youtube.com/ChemEngIQA
COURSE LINK:
https://www.chemicalengineeringguy.com/courses/petroleum-refining/
COURSE DESCRIPTION:
The main scope of the course is to create strong basis and fundamentals regarding the processes in the Petroleum Refining. We take a look to the Oil&Gas Industry briefly and continue directly with the Refining Process. We then make a focus in each individual unit operation in the refinery.
Learn about:
* Oil& Gas Industry
* Difference between Petroleum Refining vs. Petrochemical Industry
* Overview of the most important operations and products
* Market insight (supply/demand) as well as (production/consumption)
* Several Petroleum Refineries around the World
Unit Operations & Processes
* Refining and Fractionation
* Atmospheric Distillation Column
* Vacuum Distillation
* Hydrotreating (Hydrogenation)
* Blending
* Reforming
* Isomerization
* Alkylation
* Steam Cracking
* Fluid Catalytic Cracking
* Gas Sweetening (Hydrodesulfurization)
* Coking
Components:
* Fuel Gas / Natural Gas
* Liquified Petroleum Gases (LPG)
* Propane, Butane
* Sulfur / Hydrogen Sulfide
* Gasoline / Automotive Gas Oil
* Naphtha Cuts (Light/Heavy)
* Kerosene
* Diesel
* Gasoil
* Lubricants
* Vacuum Residues
* Asphalt
* Coke
NOTE: This course is focused for Process Simulation
At the end of the course you will feel confident in the Petroleum Refining Industry. You will know the most common Process & Unit Operations as well as their distribution, production and importance in daily life.
----
Please show the love! LIKE, SHARE and SUBSCRIBE!
More likes, sharings, suscribers: MORE VIDEOS!
-----
CONTACT ME
Chemical.Engineering.Guy@Gmail.com
www.ChemicalEngineeringGuy.com
http://facebook.com/Chemical.Engineering.Guy
You speak spanish? Visit my spanish channel -www.youtube.com/ChemEngIQA
COURSE LINK:
https://www.chemicalengineeringguy.com/courses/petrochemicals-an-overview/
Introduction:
The course is mainly about the petrochemical industry. Talks about several chemicals and their chemical routes in order to produce in mass scale the demands of the market.
Learn about:
Petorchemical Industry
Difference between Petroleum Refining vs. Petrochemical Industry
Paraffins, Olefins, Napthenes & Aromatics
Market insight (production, consumption, prices)
Two main Petrochemical Processes: Naphtha Steam Cracking and Fluid Catalytic Cracking
The most important grouping in petrochemical products
Petrochemical physical & chemical properties. Chemical structure, naming, uses, production, etc.
Basic Gases in the industry: Ammonia, Syngas, etc…
C1 Cuts: Methane, Formaldehyde, Methanol, Formic Acid, Urea, Chloromethanes etc…
C2 Cuts: Ethane, Acetylene, Ethylene, Ethylene Dichloride, Vinyl Chloride, Ethylene Oxide, Ethanolamines, Ethanol, Acetaldehyde, Acetic Acid, Ethylene Glycols (MEG, DEG, TEG)
C3 Cuts: Propane, Propylene, Propylene Oxide, Isopropanol, Acetone, Acrylonitrile, Propediene, Allyl chloride, Acrylic acid, Propionic Acid, Propionaldehyde, Propylene Glycol
C4 Cuts: Butanes, Butylenes, Butadiene, Butanols, MTBE (Methyl Tert Butyl Ethers)
C5 cuts: Isoprene, Pentanes, Piperylene, Cyclopentadiene, Dicyclopentadiene, Isoamyl, etc…
Aromatics: Benzene, Toluene, Xylenes (BTX), Cumene, Phenol, Ethyl Benzene, Styrene, Pthalic Anhydride, Nitrobenzene, Aniline, Benzoic Acid, Chlorobenzene, etc…
At the end of the course you will feel confident in how the petrochemical industry is established. You will know the most common petrochemicals as well as their distribution, production and importance in daily life. It will help in your future process simulations by knowing the common and economical chemical pathways.
COURSE LINK:
https://www.chemicalengineeringguy.com/courses/petrochemicals-an-overview/
Introduction:
The course is mainly about the petrochemical industry. Talks about several chemicals and their chemical routes in order to produce in mass scale the demands of the market.
Learn about:
Petorchemical Industry
Difference between Petroleum Refining vs. Petrochemical Industry
Paraffins, Olefins, Napthenes & Aromatics
Market insight (production, consumption, prices)
Two main Petrochemical Processes: Naphtha Steam Cracking and Fluid Catalytic Cracking
The most important grouping in petrochemical products
Petrochemical physical & chemical properties. Chemical structure, naming, uses, production, etc.
Basic Gases in the industry: Ammonia, Syngas, etc…
C1 Cuts: Methane, Formaldehyde, Methanol, Formic Acid, Urea, Chloromethanes etc…
C2 Cuts: Ethane, Acetylene, Ethylene, Ethylene Dichloride, Vinyl Chloride, Ethylene Oxide, Ethanolamines, Ethanol, Acetaldehyde, Acetic Acid, Ethylene Glycols (MEG, DEG, TEG)
C3 Cuts: Propane, Propylene, Propylene Oxide, Isopropanol, Acetone, Acrylonitrile, Propediene, Allyl chloride, Acrylic acid, Propionic Acid, Propionaldehyde, Propylene Glycol
C4 Cuts: Butanes, Butylenes, Butadiene, Butanols, MTBE (Methyl Tert Butyl Ethers)
C5 cuts: Isoprene, Pentanes, Piperylene, Cyclopentadiene, Dicyclopentadiene, Isoamyl, etc…
Aromatics: Benzene, Toluene, Xylenes (BTX), Cumene, Phenol, Ethyl Benzene, Styrene, Pthalic Anhydride, Nitrobenzene, Aniline, Benzoic Acid, Chlorobenzene, etc…
At the end of the course you will feel confident in how the petrochemical industry is established. You will know the most common petrochemicals as well as their distribution, production and importance in daily life. It will help in your future process simulations by knowing the common and economical chemical pathways.
This is a slideshow / resource / support material of the course.
Get full access (videlectures)
https://www.chemicalengineeringguy.com/courses/aspen-plus-bootcamp-with-12-case-studies/
x-x-x
Requirements
Basic understanding of Plant Design & Operation
Strong Chemical Engineering Fundamentals
Aspen Plus V10 (at least 7.0)
Aspen Plus – Basic Process Modeling (Very Recommended)
Aspen Plus – Intermediate Process Modeling (Somewhat Recommended)
Description
This BOOTCAMP will show you how to model and simulate common industrial Chemical Processes.
It is focused on the “BOOTCAMP” idea, in which you will learn via workshops and case studies, minimizing theory to maximize learning.
You will learn about:
Better Flowsheet manipulation and techniques
Understand Property Method Selection and its effects on simulation results
More than 15 Unit Operations that can be used in any Industry
Model Analysis Tools required for process design
Reporting Relevant Results Plot relevant data
Analysis & Optimization of Chemical Plants
Economic Analysis
Dynamic Simulations
At the end of this Bootcamp, you will be able to model more industrial processes, feel confident when modeling new processes as well as applying what you have learnt to other industries.
LINK:
https://www.chemicalengineeringguy.com/courses/aspen-plus-intermediate-course/
The INTERMEDIATE Aspen Plus Course will show you how to model and simulate more complex Processes
Analysis of Unit Operation will help you in order to simulate more complex chemical processes, as well as to analyse and optimize existing ones.
You will learn about:
- Better Flowsheet manipulation
- Hierarchy, Flowsheeting, Sub-flowsheet creation
- Logical Operators / Manipulators
- Understand Property Method Selection and its effects on simulation results
- Study of more rigorous unit operations
- Model Analysis Tools such as sensitivity and optimization
- Reporting Relevant Results Plot relevant data for Heaters, Columns ,Reactors, Pumps
- Temperature Profiles, Concentration Profile, Pump Curves, Heat Curves, etc…
- Up to 3 Case Studies (in-depth analysis)
All theory is backed up by more than 30 Practical Workshops!
At the end of the course you will be able to setup more complex processes, increase your simulation and flow sheeting techniques, run it and debugging, get relevant results and make a deeper analysis of the process for further optimization.
COURSE LINK:
https://www.chemicalengineeringguy.com/courses/gas-absorption-stripping/
Introduction:
Gas Absorption is one of the very first Mass Transfer Unit Operations studied in early process engineering. It is very important in several Separation Processes, as it is used extensively in the Chemical industry.
Understanding the concept behind Gas-Gas and Gas-Liquid mass transfer interaction will allow you to understand and model Absorbers, Strippers, Scrubbers, Washers, Bubblers, etc…
We will cover:
- REVIEW: Of Mass Transfer Basics required
- GAS-LIQUID interaction in the molecular level, the two-film theory
- ABSORPTION Theory
- Application of Absorption in the Industry
- Counter-current & Co-current Operation
- Several equipment to carry Gas-Liquid Operations
- Bubble, Spray, Packed and Tray Column equipments
- Solvent Selection
- Design & Operation of Packed Towers
- Pressure drop due to packings
- Solvent Selection
- Design & Operation of Tray Columns
- Single Component Absorption
- Single Component Stripping/Desorption
- Diluted and Concentrated Absorption
- Basics: Multicomponent Absorption
- Software Simulation for Absorption/Stripping Operations (ASPEN PLUS/HYSYS)
----
Please show the love! LIKE, SHARE and SUBSCRIBE!
More likes, sharings, suscribers: MORE VIDEOS!
-----
CONTACT ME
Chemical.Engineering.Guy@Gmail.com
www.ChemicalEngineeringGuy.com
http://facebook.com/Chemical.Engineering.Guy
You speak spanish? Visit my spanish channel -www.youtube.com/ChemEngIQA
COURSE LINK:
https://www.chemicalengineeringguy.com/courses/gas-absorption-stripping/
Introduction:
Gas Absorption is one of the very first Mass Transfer Unit Operations studied in early process engineering. It is very important in several Separation Processes, as it is used extensively in the Chemical industry.
Understanding the concept behind Gas-Gas and Gas-Liquid mass transfer interaction will allow you to understand and model Absorbers, Strippers, Scrubbers, Washers, Bubblers, etc…
We will cover:
- REVIEW: Of Mass Transfer Basics required
- GAS-LIQUID interaction in the molecular level, the two-film theory
- ABSORPTION Theory
- Application of Absorption in the Industry
- Counter-current & Co-current Operation
- Several equipment to carry Gas-Liquid Operations
- Bubble, Spray, Packed and Tray Column equipments
- Solvent Selection
- Design & Operation of Packed Towers
- Pressure drop due to packings
- Solvent Selection
- Design & Operation of Tray Columns
- Single Component Absorption
- Single Component Stripping/Desorption
- Diluted and Concentrated Absorption
- Basics: Multicomponent Absorption
- Software Simulation for Absorption/Stripping Operations (ASPEN PLUS/HYSYS)
----
Please show the love! LIKE, SHARE and SUBSCRIBE!
More likes, sharings, suscribers: MORE VIDEOS!
-----
CONTACT ME
Chemical.Engineering.Guy@Gmail.com
www.ChemicalEngineeringGuy.com
http://facebook.com/Chemical.Engineering.Guy
You speak spanish? Visit my spanish channel -www.youtube.com/ChemEngIQA
Course by Chemical Engineering Guy
Check out full course:
http://www.chemicalengineeringguy.com/courses/aspen-plus-physical-properties-course/
Ask me for special discounts, or checkout "SURPIRSE" tab in my site for special discounts.
This is course on Process Simulation will show you how to model, manipulate and report thermodynamic, transport, physical and chemical properties of substances.
You will learn about:
Physical Property Environment
Physical Property Method & Method Assistant
Fluid and Property Packages
Physical property input, modeling, estimation and regression
Thermodynamic Properties (Material/Energy balances and Thermodynamic Processes)
Transport Properties for (Mass/Heat/Momentum Transfer)
Equilibrium Properties (Vapor-Liquid, Liquid-Liquid, etc...)
Getting Results (Plots, Graphs, Tables)
This is an excellent way to get started with Aspen Plus. Understanding the physical property environment will definitively help you in the simulation and flowsheet creation!
This is a "workshop-based" course, there is about 50% theory and about 50% practice!
Get full Course here:
www.ChemicalEngineeringGuy.com/Courses
The BASIC Aspen HYSYS Course will show you how to model and simulate Processes (From Petrochemical, to Ammonia Synthesis and Polymerisation).
Analysis of Unit Operation will help you in order to optimise the Chemical Plant.
This is helpful for students, teachers, engineers and researchers in the area of R&D and Plant Design/Operation.
The course is didactic, with a lot of applied theory and Workshops/Study cases.
At the end of the course you will be able to setup a simulation, run it, get results and more important, analysis of the process for further optimization.
Chemical Engineers
Process Engineers
Students related to engineering fields
Teachers willing to learn more about process simulation
Petrochemical Engineers
The courses, subjects, labs and projects that a student must undergo in order to become a Chemical Engineer.
We divide as follows:
4 blocks:
General Engineering
Theoretical Basis
Unit Operations
Plant Design/Operation
Aspen Plus basic course for Engineers.
Introduction to Process Modeling/Simulation Software.
INDEX:
Course Objectives
Introduction to Aspen Plus
User Interface & Getting Help
Physical Properties
Introduction to Flowsheet
Unit Operation Models
Reporting Results
Case Studies I, II and III
Case Study IV
Conclusion
Applied Fluid Dynamics Course. Part 1 - Incompressible Flow
---
This is a Course Overview of Applied Fluid Dynamics Course.
The course is based in Engineering Applications
---
The course is structured in 7 Blocks
AFD1 The Mechanical Energy Equation
AFD2 Pipe, Fittings and Valves
AFD3 Energy Loss due to Friction
AFD4 Flow Measurement Equipment
AFD5 Pumps
AFD6 Incompressible Flow Applications
AFD7 Agitation and Mixing
Visit www.ChemicalEngineeringGuy.com/Courses for more information!
Automobile Management System Project Report.pdfKamal Acharya
The proposed project is developed to manage the automobile in the automobile dealer company. The main module in this project is login, automobile management, customer management, sales, complaints and reports. The first module is the login. The automobile showroom owner should login to the project for usage. The username and password are verified and if it is correct, next form opens. If the username and password are not correct, it shows the error message.
When a customer search for a automobile, if the automobile is available, they will be taken to a page that shows the details of the automobile including automobile name, automobile ID, quantity, price etc. “Automobile Management System” is useful for maintaining automobiles, customers effectively and hence helps for establishing good relation between customer and automobile organization. It contains various customized modules for effectively maintaining automobiles and stock information accurately and safely.
When the automobile is sold to the customer, stock will be reduced automatically. When a new purchase is made, stock will be increased automatically. While selecting automobiles for sale, the proposed software will automatically check for total number of available stock of that particular item, if the total stock of that particular item is less than 5, software will notify the user to purchase the particular item.
Also when the user tries to sale items which are not in stock, the system will prompt the user that the stock is not enough. Customers of this system can search for a automobile; can purchase a automobile easily by selecting fast. On the other hand the stock of automobiles can be maintained perfectly by the automobile shop manager overcoming the drawbacks of existing system.
TECHNICAL TRAINING MANUAL GENERAL FAMILIARIZATION COURSEDuvanRamosGarzon1
AIRCRAFT GENERAL
The Single Aisle is the most advanced family aircraft in service today, with fly-by-wire flight controls.
The A318, A319, A320 and A321 are twin-engine subsonic medium range aircraft.
The family offers a choice of engines
COLLEGE BUS MANAGEMENT SYSTEM PROJECT REPORT.pdfKamal Acharya
The College Bus Management system is completely developed by Visual Basic .NET Version. The application is connect with most secured database language MS SQL Server. The application is develop by using best combination of front-end and back-end languages. The application is totally design like flat user interface. This flat user interface is more attractive user interface in 2017. The application is gives more important to the system functionality. The application is to manage the student’s details, driver’s details, bus details, bus route details, bus fees details and more. The application has only one unit for admin. The admin can manage the entire application. The admin can login into the application by using username and password of the admin. The application is develop for big and small colleges. It is more user friendly for non-computer person. Even they can easily learn how to manage the application within hours. The application is more secure by the admin. The system will give an effective output for the VB.Net and SQL Server given as input to the system. The compiled java program given as input to the system, after scanning the program will generate different reports. The application generates the report for users. The admin can view and download the report of the data. The application deliver the excel format reports. Because, excel formatted reports is very easy to understand the income and expense of the college bus. This application is mainly develop for windows operating system users. In 2017, 73% of people enterprises are using windows operating system. So the application will easily install for all the windows operating system users. The application-developed size is very low. The application consumes very low space in disk. Therefore, the user can allocate very minimum local disk space for this application.
Sachpazis:Terzaghi Bearing Capacity Estimation in simple terms with Calculati...Dr.Costas Sachpazis
Terzaghi's soil bearing capacity theory, developed by Karl Terzaghi, is a fundamental principle in geotechnical engineering used to determine the bearing capacity of shallow foundations. This theory provides a method to calculate the ultimate bearing capacity of soil, which is the maximum load per unit area that the soil can support without undergoing shear failure. The Calculation HTML Code included.
Final project report on grocery store management system..pdfKamal Acharya
In today’s fast-changing business environment, it’s extremely important to be able to respond to client needs in the most effective and timely manner. If your customers wish to see your business online and have instant access to your products or services.
Online Grocery Store is an e-commerce website, which retails various grocery products. This project allows viewing various products available enables registered users to purchase desired products instantly using Paytm, UPI payment processor (Instant Pay) and also can place order by using Cash on Delivery (Pay Later) option. This project provides an easy access to Administrators and Managers to view orders placed using Pay Later and Instant Pay options.
In order to develop an e-commerce website, a number of Technologies must be studied and understood. These include multi-tiered architecture, server and client-side scripting techniques, implementation technologies, programming language (such as PHP, HTML, CSS, JavaScript) and MySQL relational databases. This is a project with the objective to develop a basic website where a consumer is provided with a shopping cart website and also to know about the technologies used to develop such a website.
This document will discuss each of the underlying technologies to create and implement an e- commerce website.
Hybrid optimization of pumped hydro system and solar- Engr. Abdul-Azeez.pdffxintegritypublishin
Advancements in technology unveil a myriad of electrical and electronic breakthroughs geared towards efficiently harnessing limited resources to meet human energy demands. The optimization of hybrid solar PV panels and pumped hydro energy supply systems plays a pivotal role in utilizing natural resources effectively. This initiative not only benefits humanity but also fosters environmental sustainability. The study investigated the design optimization of these hybrid systems, focusing on understanding solar radiation patterns, identifying geographical influences on solar radiation, formulating a mathematical model for system optimization, and determining the optimal configuration of PV panels and pumped hydro storage. Through a comparative analysis approach and eight weeks of data collection, the study addressed key research questions related to solar radiation patterns and optimal system design. The findings highlighted regions with heightened solar radiation levels, showcasing substantial potential for power generation and emphasizing the system's efficiency. Optimizing system design significantly boosted power generation, promoted renewable energy utilization, and enhanced energy storage capacity. The study underscored the benefits of optimizing hybrid solar PV panels and pumped hydro energy supply systems for sustainable energy usage. Optimizing the design of solar PV panels and pumped hydro energy supply systems as examined across diverse climatic conditions in a developing country, not only enhances power generation but also improves the integration of renewable energy sources and boosts energy storage capacities, particularly beneficial for less economically prosperous regions. Additionally, the study provides valuable insights for advancing energy research in economically viable areas. Recommendations included conducting site-specific assessments, utilizing advanced modeling tools, implementing regular maintenance protocols, and enhancing communication among system components.
Quality defects in TMT Bars, Possible causes and Potential Solutions.PrashantGoswami42
Maintaining high-quality standards in the production of TMT bars is crucial for ensuring structural integrity in construction. Addressing common defects through careful monitoring, standardized processes, and advanced technology can significantly improve the quality of TMT bars. Continuous training and adherence to quality control measures will also play a pivotal role in minimizing these defects.
Saudi Arabia stands as a titan in the global energy landscape, renowned for its abundant oil and gas resources. It's the largest exporter of petroleum and holds some of the world's most significant reserves. Let's delve into the top 10 oil and gas projects shaping Saudi Arabia's energy future in 2024.
Industrial Training at Shahjalal Fertilizer Company Limited (SFCL)MdTanvirMahtab2
This presentation is about the working procedure of Shahjalal Fertilizer Company Limited (SFCL). A Govt. owned Company of Bangladesh Chemical Industries Corporation under Ministry of Industries.
3. www.ChemicalEngineeringGuy.com
We have been studying binary systems, that is two species
For this case, the Phase Rule stated:
If given:
F as the number of degrees of freedom
C as the number of components
P as the number of phases
Then this is true:
F = C-P+2
For a Ternary (3 species in equilibrium) System, then we get:
F = C-P+2 = 3-2+2 = 3
For a Quaternary system… and so on..
F = C-P+2 = 4-2+2 = 4…
5. www.ChemicalEngineeringGuy.com
Recall that K-Value is a relationship between liquid and vapor phases:
Ki = yi/xi
According to chemistry, the hydrocarbons’ boiling point depends on their size, as
they will have mostly van der waal forces, i.e. the greater the size of the HC the
greater its boling point.
It is safe to assume that:
The larger (heavier) the HC, the greater its BP, i.e. the least volatile
If this is true:
Low boiling point HC have HIGH K-values
High boiling point HC have LOW K-values
It will now be convenient for us to work with K-Values in multicomponent systems
6. www.ChemicalEngineeringGuy.com
Verify K-Values of several Hydrocarbons
Pressure – Temperature Relationship
http://demonstrations.wolfram.com/KValueOfSeveralHydrocarbonsVersusTemperatureAndPressure/
7. www.ChemicalEngineeringGuy.com
For light hydrocarbons, the value of Ki of each species can be obtained from the
graph (called the “K chart”) prepared by DePriester
The temperature and pressure of the system must specified
Note that each plot/graph of each hydrocarbons can be written in the form of
equation:
X values vary from substance to substance and the units being used
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
8. www.ChemicalEngineeringGuy.com
Input variables:
Set a Temperature
Set a Pressure
Set a component
Output variable
K-Value
As you will see, if T/P are fixed, then, for pure substances:
There is only a SINGLE line that describes these characteristic
10. www.ChemicalEngineeringGuy.com
If we set T/P:
There is a unique
condition for a PURE
substance
See Lines:
Orange (high P– Low T)
Yellow (high P– high T)
Blue (low P– Low T)
Red (Low P– high T)
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
11. www.ChemicalEngineeringGuy.com
Use the animation to verify certain conditions.
Methane
Propane
Octane
http://demonstrations.wolfram.com/DePriesterChartForHydrocarbons/
13. www.ChemicalEngineeringGuy.com
If the specifications that you are given for your single-stage equilibrium separations
process are not T and P alone but say:
V/F = 0 and T or P
(which is a bubble point temperature or pressure, respectively)
or V/F = 0 and T or P
(which is a dew point temperature or pressure, respectively)
Do NOT use Rachford-Rice Equation!
In this case, we will have something between 0 < V/F <1
14. www.ChemicalEngineeringGuy.com
Let us first consider bubble point calculations
In this case the liquid-phase composition xi is given
it corresponds to the case where V is very small and
Recall:
The bubble point of a liquid is the point where the liquid just starts to evaporate (boil),
that is, when the first vapor bubble is formed.
If the temperature is given:
then we must lower the pressure until the first bubble is formed.
If the pressure is given:
then we must increase the temperature until the first bubble is formed.
0V
i ix z
1i iK x
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
15. www.ChemicalEngineeringGuy.com
NOTE:In both cases, this corresponds to adjusting T or p until the computed sum of
vapor fractions is just 1, that is,
Since:
Then
1iy
i
i i i i
i
y
K y K x
x
1i iK x
16. www.ChemicalEngineeringGuy.com
At bubble point, V/F = 0, by definition in equilibrium
From the equation:
Step 1: Guess any Bubble Point Temperature
Step 2: Determine K-values from the Chart/Equation/Table/Plot
Step 3: If the function ( ) then Bubble Point is correct
Step 4: If the function is not 1 change Bubble point accordingly:
function >1 reduce T
function < 1 increase T
Step 5: Repeat Iteration until % error is met
Tip:
Best Educated Guess is
1i iK x 1i iK z
i ix z
1i iK z
old
new
i i
K
K
K z
17. www.ChemicalEngineeringGuy.com
Bubble point at given temperature T.
A liquid mixture contains 50% pentane (1), 30% hexane (2) and 20% cyclohexane (3)
(all in mol-%), i.e.,
At T = 400 K, the pressure is gradually decreased.
What is the bubble pressure and composition of the first vapor that is formed?
Assume ideal liquid mixture and ideal gas (Raoult’s law).
1 2 30.5; 0.3; 0.2x x x
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
18. www.ChemicalEngineeringGuy.com
Solution.
The task is to find a Pressure that satisfies
Since T is given, this is trivial (not required)
We can simply calculate P from the previous equation
We start by computing the vapor pressures for the three components at T = 400K.
Using the Antoine data, we get:
At the bubble point, the liquid phase composition is given, so the partial pressure of
each component is
( )i ix P T p
1
2
3
( 400 ) 10.248
( 400 ) 4.647
( 400 ) 3.358
P T K bar
P T K bar
P T K bar
1 1 1
2 2 2
3 3 3
(0.5)(10.248 ) 5.124
(0.3)(4.647 ) 1.394
(0.2)(3.358 ) 0.672bar
p x P bar bar
p x P bar bar
p x P bar
19. www.ChemicalEngineeringGuy.com
Thus, from the equation of the bubble pressure we get:
Finally, the vapor composition (composition of the first vapor bubble) is
1 2 3 7.189p p p p bar
1
1
2
2
3
3
5.124
0.713
7.189
1.394
0.194
7.189
0.672
0.093
7.189
p bar
y
p bar
p bar
y
p bar
p bar
y
p bar
20. www.ChemicalEngineeringGuy.com
A hydrocarbon liquid mix with
Composition (10,20,30,40% mol of; nC3, nC4, nC5, nC6)
Find the temperature at which we will get the first bubble formation.
Do NOT Assume ideal solution/gas
/ 0, 700V F P kPa
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
23. www.ChemicalEngineeringGuy.com
Step 2. Read K values
3
4
5
6
390
nC
nC
nC
nC
K
K
K
K
T F
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
25. www.ChemicalEngineeringGuy.com
Step 3. Use f(x) function
Step 4. K-value is Not what we expected
Guess new T… Recommended is to: Normalize (divide by K function value)
Do this for the smallest (MVC) Propane
Repeat Iteration!
( ) 3.69i iF x K Z
3 3 4 4 5 5 6 6
3 4 5 6
(0.10) (0.20) (0.30) (0.40)
(9.8)(0.10) (5.7)(0.20) (3.1)(0.30) (1.8)(0.40)
3.70
i i nC nC nC nC nC nC nC nC
i i nC nC nC nC
i i
i i
K Z K Z K Z K Z K Z
K Z K K K K
K Z
K Z
9.8
2.66
3.7
K
27. www.ChemicalEngineeringGuy.com
Step 2. Read K values
3
4
5
6
2.66
0.80
0.30
0.12
128
nC
nC
nC
nC
K
K
K
K
T F
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
28. www.ChemicalEngineeringGuy.com
Step 3. Use f(x) function
Step 4. K-value is Not what we expected
Normalize (divide by K function value)
Do this for the smallest (MVC) Propane
Repeat Iteration!
( ) 0.61i iF x K Z
3 3 4 4 5 5 6 6
3 4 5 6
(0.10) (0.20) (0.30) (0.40)
(2.66)(0.10) (0.80)(0.20) (0.3)(0.30) (0.12)(0.40)
0.61
i i nC nC nC nC nC nC nC nC
i i nC nC nC nC
i i
i i
K Z K Z K Z K Z K Z
K Z K K K K
K Z
K Z
2.66
4.36
0.61
K
30. www.ChemicalEngineeringGuy.com
Step 3. Use f(x) function
Step 4. K-value is Not what we expected
Normalize (divide by K function value)
Do this for the smallest (MVC) Propane
Repeat Iteration!
( ) 1.18i iF x K Z
3 3 4 4 5 5 6 6
3 4 5 6
(0.10) (0.20) (0.30) (0.40)
(4.36)(0.10) (1.80)(0.20) (0.85)(0.30) (0.36)(0.40)
1.18
i i nC nC nC nC nC nC nC nC
i i nC nC nC nC
i i
i i
K Z K Z K Z K Z K Z
K Z K K K K
K Z
K Z
4.36
3.70
1.20
K
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
32. www.ChemicalEngineeringGuy.com
Step 3. Use f(x) function
Step 4. K-value is Not what we expected
Normalize (divide by K function value)
Do this for the smallest (MVC) Propane
Repeat Iteration!
( ) 0.93i iF x K Z
3.68
3.94
0.93
K
33. www.ChemicalEngineeringGuy.com
Step 2. Read K values
3
4
5
6
3.94
1.40
0.60
0.27
188
nC
nC
nC
nC
K
K
K
K
T F
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
35. www.ChemicalEngineeringGuy.com
Let us next consider dew point calculations.
In this case the vapor-phase composition yi is given
(it corresponds to the case where L is very small ( ) and
The dew point of a vapor (gas) is the point where the vapor just begins to condense,
that is, when the first liquid drop is formed.
If the temperature is given
then we must increase the pressure until the first liquid is formed.
If the pressure is given
then we must decrease the temperature until the first liquid is formed.
0L i iy z
36. www.ChemicalEngineeringGuy.com
In both cases, this corresponds to adjusting T or p until
Or, more conveniently:
1ix
1i
i
y
K
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
37. www.ChemicalEngineeringGuy.com
At the dew point, by definition, and from f(1) = 0, we can find:
If this is true, then, when P and T are given:
Must be changed since T is too large… The steps are as follows:
Step 1. Guess any Dew Point Temperature
Step 2: Determine the K-values based on that
Step 3. Calculate . If function is not near 1, then:
Increase T when Function is less than 1.
Decrease T when Function is greater than 1.
Step 4. Recalculate New K-values based on normalization of K-old
Step 5. Repeat Iteration until acceptable % error value.
1i
i
Z
K
1i
i
Z
K
/ 1V F
1i
i
Z
K
38. www.ChemicalEngineeringGuy.com
Calculate the Dew point at given Temperature T.
A vapor mixture contains:
50% pentane (1), 30% hexane (2) and 20% cyclohexane (3) (all in mol-%), i.e.,
At T = 400 K, the pressure is gradually increased.
What is the dew point pressure and the composition of the first liquid that is
formed?
Assume ideal liquid mixture and ideal gas (Raoult’s law).
1 2 30.5; 0.3; 0.2y y y
39. www.ChemicalEngineeringGuy.com
Solution.
The task is to find the value of p that satisfies
Since T is given, this is trivial; we can simply calculate 1/p from (7.48).
From previous experiments and data, we got the following regression:
and we find
The liquid phase composition is:
Then, we find
1
( )
i
i
y
P T p
11 0.5 0.3 0.2
0.1729
10.248 4.647 3.358
bar
p
5.75p bar 1
( )
i
i
i
y
x
P T p
1 2 3
0.5 5.78 0.3 5.78 0.2 5.78
0.282; 0.373; 0.345
10.248 4.647 3.749
x x x
x x x
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
40. www.ChemicalEngineeringGuy.com
For the previous mixture of Bubble Point:
Calculate its Dew Point
That is, assume it is a vapor
You are looking for condensation point
41. www.ChemicalEngineeringGuy.com
Component / Molar flow
C1 20
C2 15
C3 12
C4 15
IC4 12
NC5 15
IC5 10
C6 5
C7 3
• A) Get Dew point @ T= ? P = 50bar
• B) Get Bubble point @ T= 220°C, P = 10bar
• C) What phase do we have at 25/25
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
42. www.ChemicalEngineeringGuy.com
Component / Molar flow
B 0.25
T 0.25
O-X 0.25
P-X 0.25
• A) Get Dew point @ T= 150°C, P = 50bar
• B) Get Dew point @ T= 220°C, P = 10bar
• C) What is the Critical Point & Meaning?
44. www.ChemicalEngineeringGuy.com
Next, consider a flash where a feed F (with composition zi) is split into
A vapor product V (with composition yi)
A liquid product (with composition xi)
For each of the Nc components, we can write a material balance:
In addition, the vapor and liquid is assumed to be in equilibrium,
i i iFz Lx Vy
i i iy K x
45. www.ChemicalEngineeringGuy.com
The K-values:
Must be computed from the VLE model.
In addition, we have the two relationships:
With a given feed (F, zi), we then have:
3Nc + 2 equations
3Nc + 4 unknowns (xi , yi , Ki , L, V, T, p).
Thus, we need two additional specifications, and with these the equation set should
be solvable
, ,( ),i i i iK K T P x y
1
1
1
i
i
i i
x
y
x y
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
46. www.ChemicalEngineeringGuy.com
The simplest flash is usually to specify p and T (pT-flash)
because Ki depends mainly on p and T .
Let us show one common approach for solving the resulting equations, which has
good numerical properties.
Substituting into the mass balance:
Gives
Solving with respect to xi gives:
Simplify via L = F − L (total mass balance) to derive
i i iFz Lx Vy
i i iy K x
(K )i i i iFz Lx V x
( )
( ) (1)
( ) 1 ( 1)
1 ( 1)
i i i
i i
i V
Fi i
V
F
i
i
i
Fz x L VK
L F z z
x
L V K K
z
x
K
47. www.ChemicalEngineeringGuy.com
Here, we cannot directly calculate xi because the vapor split V /F is not known.
To find V /F we may use:
the relationship
alternatively
OR the addition of both…
However, it has been found that the combination Σi(yi−xi) = 0
It results in an equation with good numerical properties
This is the so-called Rachford-Rice Flash Equation
1
1
1
i
i
i i
x
y
x y
isat
i
p T
K
p
( 1)
0
1 ( 1)
i i
i
z K
K
48. www.ChemicalEngineeringGuy.com
Rachford-Rice Equation:
Is a monotonic function in V/F
It is easy to solve numerically.
A physical solution must satisfy 0 ≤ V /F ≤ 1.
If we assume that Raoult’s holds, then Ki depends on p and T only.
Then, with T and p specified, we know Ki and the Rachford-Rice equation can be
solved for V /F.
For non-ideal cases, Ki depends also on xi and yi
One approach is add an outer iteration loop on Ki .
isat
i
p T
K
p
49. www.ChemicalEngineeringGuy.com
This will be the typical procedure for the RRE
Note that this is based on a numerical method
Newton-Raphson Method
Uses the original function, f(phi)
It also requires the derivative of the function, f’(phi)
( 1)
( )
1 ( 1)
i i
i
z K
f
K
0.50
V
F
2
2
(1 )
'( )
[1 ( 1)]
i i
i
z K
f
K
( , , , ... )i j k zF z z z z
(V,y ,y ,y ...y )i j k z
(L,x ,x ,x ...x )i j k z
( , )T P
( , , ... )i j k zK K K K
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
50. www.ChemicalEngineeringGuy.com
1. Given F, zi, T and P
2. Get Ki for species (either graph, equations or experimental values)
Antoine Equation (ideal)
K-Values from DePriester Chart
3. Assume a phi value (vaporized material in the feed) (hint good start is 0.5)
4. Get the Numerical Value of Rachford Rice Equation
Example:
BTX ( Benzene, Toluene, Xylene) System:
( 1)
0
1 ( 1)
i i
i
z K
K
0.50
V
F
(1 )(1 ) (1 )
( )
1 ( 1) 1 ( 1) 1 ( 1)
xylene xylenebenzene benzene toluene toluene
benzene toluene xylene
z Kz K z K
f
K K K
51. www.ChemicalEngineeringGuy.com
5. Get the Numerical Value of the Derivative of Rachford Rice Equation
Example:
BTX ( Benzene, Toluene, Xylene) System:
V
F
22 2
2 2 2
(1 )(1 ) (1 )
'( )
[1 ( 1)] [1 ( 1)] [1 ( 1)]
xylene xylenebenzene benzene toluene toluene
benzene toluene xylenei
z Kz K z K
f
K K K
2
2
(1 )
'( )
[1 ( 1)]
i i
i
z K
f
K
52. www.ChemicalEngineeringGuy.com
6. Recalculate phi (Newton Raphson Method)
7. Verify Rel. Error, if < 0.0001, this is ok, otherwise go to step 3 (repeat iteration)
V
F
( )
'( )
old
new old
old
f
f
% .error 100%new old
old
rel abs x
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
53. www.ChemicalEngineeringGuy.com
8. Get V, L, xi, and yi (see equations)
Note that in all cases:
You will need K and phi
V V F
L L F V
1 ( 1)
1 ( 1)
i i
i
i
i
i
i
K z
y
K
z
x
K
V
F
54. www.ChemicalEngineeringGuy.com
Given a Flash with the following data:
Composition (zi)
(BTX, 0.60, 0.25, 0.15)
VLE (Antoine Constant) Data:
A) Get the compositions, flow rates of Vapor & Liquid streams
i A B C
B 6.879 1196.700 219.160
T 6.950 1342.000 219.190
X 7.000 1476.390 213.870
1 , 100
100
&
kmol
h
P atm T C
F
V L unknown
55. www.ChemicalEngineeringGuy.com
Step 1 – Get the given Data:
1 , 100 , 100
0.6; 0.25, 0.15
kmol
h
benzene toluene xylene
P atm T C F
Z Z Z
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
56. www.ChemicalEngineeringGuy.com
Step 2 Get Ki-values
Via Raoult’s Law
Via DePriester Diagrams (not available for BTX)
If we use Raoult’s Law & Antoine’s Equation:
1.7756
0.7322
0.2611
benzene
toluene
xylene
K
K
K
58. www.ChemicalEngineeringGuy.com
Step 4. Calculate The Value of the Rachford-Rice Equaiton (RRE)
0.5
(1 )
( )
1 ( 1)
(1 )(1 ) (1 )
( )
1 ( 1) 1 ( 1) 1 ( 1)
0.60(1 1.7756) 0.25(1 0.7322)
( )
1 0.50(1.7756 1) 1 0.50(0.732
i i
i
xylene xylenebenzene benzene toluene toluene
benzene toluene xylenei
z K
f
K
z Kz K z K
f
K K K
f
0.15(1 0.2611)
2 1) 1 0.50(0.2611 1)
( ) 0.0823f
59. www.ChemicalEngineeringGuy.com
Step 5. Calculate The Value of the derivative of RRE
2
2
22 2
2 2 2
2
2
0.5
(1 )
'( )
[1 ( 1)]
(1 )(1 ) (1 )
'( )
[1 ( 1)] [1 ( 1)] [1 ( 1)]
0.60(1 1.7756) 0.25
'( )
1 0.50(1.7756 1)]
i i
i
xylene xylenebenzene benzene toluene toluene
benzene toluene xylenei
z K
f
K
z Kz K z K
f
K K K
f
2 2
2 2
(1 0.7322) 0.15(1 0.2611)
1 0.50(0.7322 1)] 1 0.50(0.2611 1)]
'( ) 0.4172f
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
61. www.ChemicalEngineeringGuy.com
Step 7. Verify phi value (error)
Error is too large, repeat from step 3
% . 100%
0.6972
% . 100%
0.5000
% . 139%
new
old
rel error x
rel error x
rel error
62. www.ChemicalEngineeringGuy.com
The most convenient way to do this is via a Spreadsheet… as we will need to iterate
Step 7. Verify phi value (error)
Best Case phi = 0.6806; error is acceptable
Trial phi f(1) f(2) f(3) f(phi) f'(1) f'(2) f'(3) f'(phi) New Phi %error
1 0.5 -0.33532 0.0773 0.175775 -0.08225 0.187402 0.023901 0.205979 0.417282 0.6971 39.42
2 0.6971 -0.30205 0.08232 0.228567 0.008834 0.152057 0.027105 0.348286 0.527447 0.6804 2.40
3 0.6804 -0.30462 0.08187 0.222879 0.000126 0.154654 0.026808 0.026808 0.20827 0.6797 0.09
4 0.6797 -0.30471 0.08185 0.222679 -0.00018 0.154749 0.026797 0.026797 0.208344 0.6806 0.13
5 0.6806 -0.30458 0.08187 0.222971 0.000269 0.154611 0.026813 0.026813 0.208236 0.6793 0.19
6 0.6793 -0.30478 0.08184 0.222544 -0.00039 0.154813 0.02679 0.02679 0.208394 0.6812 0.28
7 0.6812 -0.30448 0.08189 0.223167 0.000572 0.154518 0.026823 0.026823 0.208164 0.6785 0.40
2
2
22 2
2 2 2
2
2
0.5
(1 )
'( )
[1 ( 1)]
(1 )(1 ) (1 )
'( )
[1 ( 1)] [1 ( 1)] [1 ( 1)]
0.60(1 1.7756) 0.25
'( )
1 0.50(1.7756 1)]
i i
i
xylene xylenebenzene benzene toluene toluene
benzene toluene xylenei
z K
f
K
z Kz K z K
f
K K K
f
2 2
2 2
(1 0.7322) 0.15(1 0.2611)
1 0.50(0.7322 1)] 1 0.50(0.2611 1)]
'( ) 0.4172f
f’(1) f’(2) f’(3)
0.5
(1 )
( )
1 ( 1)
(1 )(1 ) (1 )
( )
1 ( 1) 1 ( 1) 1 ( 1)
0.60(1 1.7756) 0.25(1 0.7322)
( )
1 0.50(1.7756 1) 1 0.50(0.732
i i
i
xylene xylenebenzene benzene toluene toluene
benzene toluene xylenei
z K
f
K
z Kz K z K
f
K K K
f
0.15(1 0.2611)
2 1) 1 0.50(0.2611 1)
( ) 0.0823f
f(1) f(2) f(3)
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
63. www.ChemicalEngineeringGuy.com
Step 8. Calculate all other Values
For compositions, use Spreadsheet
(0.6803)(100) 68.03 /
100 68.03 31.97 /
V V F V kmol h
L L F V kmol h
1 ( 1)
1 ( 1)
i i
i
i
i
i
i
K z
y
K
z
x
K
64. www.ChemicalEngineeringGuy.com
Step 8. Calculate all other Values
1 ( 1)
1 ( 1)
i i
i
i
i
i
i
K z
y
K
z
x
K
Species i Ki zi phi yi xi
Benzene 1 1.78 0.60 0.6806 0.69728 0.392703
Toluene 2 0.73 0.25 0.6806 0.22385 0.305722
Xylene 3 0.26 0.15 0.6806 0.07879 0.301747
65. www.ChemicalEngineeringGuy.com
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
66. www.ChemicalEngineeringGuy.com
A feed:
(1) 20 mol % ethane
(2) 20 mol % isobutane
(3) 20 mol % n-pentane
(4) 40 mol % n-hexane
Flash Operation is at T = 100°c, P = 600kPa
A) What mole fraction of the feed is vaporized?
B) Composition of vapor?
67. www.ChemicalEngineeringGuy.com
Step 1: Calculate K Values
F = must be assumed, 100
Z = given, 0.2,0.20,0.20,0.40
Given, 100°C (212F), 600kPa (87 psi)
Step 2. Calculate K Values
Use DePriester Chart.
Ethane 12.5
isobutane 2.80
n-pentane 0.95
n-hexane 0.45
68. www.ChemicalEngineeringGuy.com
Step 3. Assume phi-values
0.50
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
70. www.ChemicalEngineeringGuy.com
Step 7. Verify if error is acceptable.
V/F = 0.7597
A) Percentage of Vapor = 75.97%
Trial phi f(1) f(2) f(3) f(4) f(phi) f'(1) f'(2) f'(3) f'(4) f'(phi) New Phi %error
1 0.500 -0.34074 -0.1895 0.010256 0.303448 -0.21651 0.580521 0.179501 0.000526 0.230202 0.990751 0.7185 43.71
2 0.7185 -0.2483 -0.157 0.010373 0.363752 -0.03115 0.308257 0.123206 0.000538 0.330788 0.762789 0.7594 5.68
3 0.7594 -0.23632 -0.1521 0.010395 0.37778 -0.00024 0.279228 0.115673 0.115673 0.356794 0.867368 0.7596 0.04
4 0.7596 -0.23624 -0.1521 0.010395 0.37788 -3.2E-05 0.279044 0.115624 0.115624 0.356983 0.867274 0.7597 0.00
5 0.7597 -0.23623 -0.1521 0.010395 0.377893 -4.3E-06 0.279019 0.115617 0.115617 0.357008 0.867262 0.7597 0.00
6 0.7597 -0.23623 -0.1521 0.010395 0.377895 -5.7E-07 0.279016 0.115616 0.115616 0.357011 0.86726 0.7597 0.00
7 0.7597 -0.23623 -0.1521 0.010395 0.377895 -7.5E-08 0.279016 0.115616 0.115616 0.357012 0.86726 0.7597 0.00
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
71. www.ChemicalEngineeringGuy.com
B) Composition of vapor?
Species i Ki zi phi yi xi
Ethane 1 12.5 0.20 0.7597 0.256764 0.020541
i-Butane 2 2.8 0.2 0.7597 0.23654 0.084479
n-Pentane 3 0.95 0.2 0.7597 0.197502 0.207897
n-Hexane 4 0.45 0.4 0.7597 0.309191 0.68709
0.999998 1.000007
(0.7597)(100) 75.97 /
100 75.97 24.03 /
V V F V mol h
L L F V kmol h
1 ( 1)
1 ( 1)
i i
i
i
i
i
i
K z
y
K
z
x
K
72. www.ChemicalEngineeringGuy.com
For a mix at T= 95°C and P = 700kPa
The composition of 40, 30, 20, 10 mol percent:
propane (1)
n-butane (2)
n-pentane (3)
n-hexane (4)
A) What percentage of the feed enters as liquid?
73. www.ChemicalEngineeringGuy.com
Step 1. Get data
F, T, P, zi are given!
T= 95°C = 203°F
P = 700kPa = 101 psi
Step 2. Get Ki
From K-chart:
4.20
1.75
0.74
0.34
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
75. www.ChemicalEngineeringGuy.com
Step 6: Verify, iterate
NOTE
If The Value of RRE < 0, this is above the bubble point… WHY?
If the Value of RRE derivative > RRE, this is ABOVE the dew point…
Trick question… This is all VAPOR!
phi 0.5
i zi Ki f(phi) f'(phi)
1 0.4 4.2 -1.28 4.096
2 0.3 1.75 -0.225 0.16875
3 0.2 0.74 0.052 0.01352
4 0.1 0.34 0.066 0.04356
Sum = -1.387 4.32183
76. www.ChemicalEngineeringGuy.com
In the following animation:
Change the Flash Pressure
See the Effect of Q in temperature
Compare the volatility of species:
Butane vs. heptane
https://demonstrations.wolfram.com/FlashDistillationOfAMixtureOfFourHydrocarbons/
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website:
77. www.ChemicalEngineeringGuy.com
Use Aspen Plus Software to Simulate Ex 1. Rachford-Rice Flashing
A) Verify Composition & Streams
B) Use Physical Property Analysis:
PV-Curve
Mixture Properties
C) Use Sensitivity Analysis for:
Effect of Temperature in Vapor
Tmin? WHY
Tmax? WHY
78. www.ChemicalEngineeringGuy.com
Phi = 0.7597
Species i Ki zi phi yi xi
Ethane 1 12.5 0.20 0.7597 0.256764 0.020541
i-Butane 2 2.8 0.2 0.7597 0.23654 0.084479
n-Pentane 3 0.95 0.2 0.7597 0.197502 0.207897
n-Hexane 4 0.45 0.4 0.7597 0.309191 0.68709
0.999998 1.000007
(0.7597)(100) 75.97 /
100 75.97 24.03 /
V V F V mol h
L L F V kmol h
Trial phi f(1) f(2) f(3) f(4) f(phi) f'(1) f'(2) f'(3) f'(4) f'(phi) New Phi %error
1 0.500 -0.34074 -0.1895 0.010256 0.303448 -0.21651 0.580521 0.179501 0.000526 0.230202 0.990751 0.7185 43.71
2 0.7185 -0.2483 -0.157 0.010373 0.363752 -0.03115 0.308257 0.123206 0.000538 0.330788 0.762789 0.7594 5.68
3 0.7594 -0.23632 -0.1521 0.010395 0.37778 -0.00024 0.279228 0.115673 0.115673 0.356794 0.867368 0.7596 0.04
4 0.7596 -0.23624 -0.1521 0.010395 0.37788 -3.2E-05 0.279044 0.115624 0.115624 0.356983 0.867274 0.7597 0.00
5 0.7597 -0.23623 -0.1521 0.010395 0.377893 -4.3E-06 0.279019 0.115617 0.115617 0.357008 0.867262 0.7597 0.00
6 0.7597 -0.23623 -0.1521 0.010395 0.377895 -5.7E-07 0.279016 0.115616 0.115616 0.357011 0.86726 0.7597 0.00
7 0.7597 -0.23623 -0.1521 0.010395 0.377895 -7.5E-08 0.279016 0.115616 0.115616 0.357012 0.86726 0.7597 0.00
Do you need the Full Version?
Contact me if needed!
Contact@ChemicalEngineeringGuy.com
https://courses.chemicalengineeringguy.com/courses
You can also check out more content here:
My Youtube Channel
My Fan Page
The LinkedIn
My website: