Petrochemical Engineering

Petroleum industry has a major share in the world energy and industrial markets. In the recent
years, petroleum industry has grown increasingly complex as a result of tighter competition,
stricter environmental regulations and lower-margin profits. It is facing a challenging task to
remain competitive in a globalized market, the fluctuating demand for petroleum products and the
current situation of fluctuating high petroleum crude oil prices is a demonstration that markets
and industries throughout the world are impacted by the uncertainty and volatility of the
petroleum industry.
These factors and others forced petroleum companies for a greater need in the strategic planning
optimization and sensitivity analysis in order to make decisions that satisfy conflicting multiobjective goals of maximizing expected profit while simultaneously minimizing risk. These
decisions have to take into account uncertainties and constraints in factors such as the source and
availability of raw material, production and distribution costs and expected market demand.
This book discusses the full aspects concerning the Petroleum Refinery starting from its history
reaching a plant design for the products refinery processes and naphtha processing with the help
of an industrial simulation programs such as Aspen HYSYS. It covers refinery classification, crude
oil structure and economics, in addition to the refinery processing line from the beginning of the
handling of the feed introduced to plant units passing through the desalting, preheating, flashing
units till reaching the separation processes in distillation towers producing the refinery products,
vacuum tower distillation and the naphtha processing using the modern technique Methaforming
that are all discussed theoretically and simulated for a real-life Petroleum Plant Production Units
using the industrial simulating programs.
This finally demonstrate the full image of the petroleum refinery processes importance to the local
and international world of petroleum and petrochemical industries and human’s life.

Los catalizadores provocan reacciones químicas o aceleran la velocidad a la que una reacción se acerca al equilibrio. El catalizador proporciona una superficie adecuada para que los reactivos se adsorban y para que los productos se desorban. El papel del catalizador es reducir la energía de activación de una reacción, proporcionando una vía de reacción adecuada y que se aplica a todos los tipos de catálisis, es decir, catálisis homogéneas, heterogéneas y enzimáticas.

Principles of Pre-reforming Technology
Pre-reforming
Flow-schemes
Feed-stocks
Catalyst handling, loading & start-up
Benefits of a pre-reformer
Case studies
Effects upon primary reformer
Data analysis
Reactor temperature profiles
Catalyst management
Summary

Methanol Plant - Theory of Distillation
Principles of Distillation
Distillation Theory
Flowsheet Description
Topping Column Details
Topping Column Operation
Refining Column Details
Refining Column Operation
Distillation Control
Distillation Problems

Methanol Plant Safety Experiences in the last Twenty Years
If it can go wrong – it will
If something looks odd – it is
Apparent safe systems can fail
Issues include
Metal dusting
Methanol or hydrogen fires
Intent changes
Methanation
“Safe Systems”

Fire and Explosion Hazardous Properties of Breakers Applied in the Processes of Oil Production Stimulation
Применение в процессах нефтедобычи большого спектра химических реагентов требует изучения их
свойств, которые представляют основную опасность при использовании, транспортировке, хранении и
испытаниях. В статье исследуются пожароопасные и взрывоопасные свойства брейкеров, применяемых в
процессах интенсификации нефтедобычи для деструкции полимерных гелей, использующихся для гидроразрыва пласта. Опасность брейкеров обусловлена сильными окислительными свойствами и интенсивным
самоускоряющимся разложением с выделением газообразных веществ при нагревании. Представленный
материал содержит краткую характеристику брейкеров по химическому составу, свойствам и применению,
приведены результаты испытаний брейкеров с определением показателей пожароопасности, взрывоопасности по чувствительности к удару и оценкой термического разложения. Сделан вывод об обусловленности
пожароопасных свойств брейкеров прежде всего окислительными свойствами пероксидов, входящих в их
состав.
Ключевые слова: пожароопасность химреагентов для нефтяной отрасли, гидравлический разрыв пласта (ГРП), брейкер для гидравлического разрыва пласта, деструктор полимерных гелей, безопасность нефтедобычи, пероксиды в нефтепромысловой химии, повышение нефтеотдачи пластов, лабораторные испытания
нефтепромысловой химии.

Calculation of an Ammonia Plant Energy Consumption: 
Case Study: #06023300
Plant Note Book Series: PNBS-0602
CONTENTS
0 SCOPE
1 CALCULATION OF NATURAL GAS PROCESS FEED CONSUMPTION
2 CALCULATION OF NATURAL GAS PROCESS FUEL CONSUMPTION
3 CALCULATION OF NATURAL GAS CONSUMPTION FOR PILOT BURNERS OF FLARES
4 CALCULATION OF DEMIN. WATER FROM DEMIN. UNIT
5 CALCULATION OF DEMIN. WATER TO PACKAGE BOILERS
6 CALCULATION OF MP STEAM EXPORT
7 CALCULATION OF LP STEAM IMPORT
8 DETERMINATION OF ELECTRIC POWER CONSUMPTION
9 DETERMINATION OF THE TOTAL ENERGY CONSUMPTION OF THE AMMONIA PLANT ISBL
10 ADJUSTMENT OF ELECTRIC POWER CONSUMPTION FOR TEST RUN CONDITIONS
11 CALCULATION OF AMMONIA SHARE IN MP STEAM CONSUMPTION IN UTILITIES
12 CALCULATION OF AMMONIA SHARE IN ELECTRIC POWER CONSUMPTION IN UTILITIES
13 DETERMINATION OF THE TOTAL ENERGY CONSUMPTION OF THE AMMONIA PLANT OSBL
14 DETERMINATION OF THE TOTAL ENERGY CONSUMPTION OF THE AMMONIA PLANT

HYDROGENATION REACTOR DESIGN - Fixed Bed Reactor Internals
The following is designed to give an overview on and some insight in the general design features of hydrogenation reactors and the impact of the various reactor internals on performance.

El articulo demuestra que la construcción de las plantas de Tiourea y fertilizantes NPK y DAP en el Complejo Petroquímico de Bulo–Bulo de Cochabamba, Bolivia, pueden ser una realidad a corto plazo, porque son derivados de la urea y amoniaco que reproducirán a partir de Junio 2016. La tiourea es un agente lixiviante no–tóxico para la recuperación de oro, substituyendo al cianuro que sumamente toxico. La producción de fertilizantes NPK y DAP baratos en Bolivia beneficiará a miles de agricultores bolivianos porque podrá incrementar considerablemente su producción y se revertirá la situación de importación de dichos fertilizantes con precios muy altos y prohibitivos; solo así Bolivia tendrá suficiente producción de alimentos para garantizar la seguridad alimentaria del país.

Glyoxal is provided generally as a four-hundredth solution. it's oftentimes used for condensation and cross-linking reactions owing to the reactivity of its organic compound teams towards polyfunctional compounds with group or amino teams, e.g. with organic compound and its derivatives, or with starch, cellulose, cotton, casein, or animal product. It acts as a biologically active compound, inhibits corrosion, and aids in solidifying rubber and in animal skin tanning. it's associate intermediate within the preparation of dyes, prescription drugs, polymers and textile auxiliaries. industrial glyoxal is ready by either the gas section reaction of ethanediol within the presence of a silver or copper catalyst or by the liquid section reaction of ethanal with acid. The potential of manufacturing glyoxal from the ethanediol is encouraging and may be any explored particularly within the country with the high ethanediol productivity Keywords-Oxidation of ethylene glycol, Condensation and cross linking reactions.

Ammonia Plant Technology
Pre-Commissioning Best Practices:
Piping and Vessels Flushing and Cleaning Procedure
CONTENTS
1 Scope
2 Aim/purpose
3 Responsibilities
4 Procedure
4.1 Main cleaning methods
4.1.1 Mechanical cleaning
4.1.2 Cleaning with air
4.1.3 Cleaning with steam (for steam networks only)
4.1.4 Cleaning with water
4.2 Choice of the cleaning method
4.3 Cleaning preparation
4.4 Protection of the devices included in the network
4.5 Protection of devices in the vicinity of the network
4.6 Water flushing procedure
4.6.1 Specific problems of water flushing
4.6.2 Preparation for water flushing
4.6.3 Performing a water flush
4.6.4 Cleanliness criteria
4.7 Air blowing procedure
4.7.1 Specific problems of air blowing
4.7.2 Preparation for air blowing
4.7.3 Performing air blowing
4.7.4 Cleanliness checks
4.8 Steam blowing procedure
4.8.1 Specific problems of steam blowing
4.8.2 Preparation for steam blowing
4.8.3 Performing steam blowing
4.8.4 Cleanliness checks
4.9 Chemical cleaning procedure
4.9.1 Specific problems of cleaning with a chemical solution
4.9.2 Preparation for chemical cleaning
4.9.3 Performing a chemical cleaning
4.9.4 Cleanliness criteria
4.10 Re-assembly - general guideline
4.11 Preservation of flushed piping

La raffinerie de Skikda est l'une des plus importantes industries pour Economie nationale car elle couvre la région centre du pays avec ces différents produits finis ou semi finis, elle repose essentiellement sur la distillation atmosphérique l'unité de platforming et l'unité de Gas-plant. Cette unité a pour rôle la valorisation de propane et de
butane.L’installation est située dans la zone industrielle de Skikda d’environ 120 km à partir de l’aéroport le plus proche (Annaba/Constantine) en Algérie. La raffinerie est en opération depuis 1979.
Sonatrach s’est engagé à rénover et améliorer leur raffinerie existante à Skikda en Algérie, sous “le Projet de Réhabilitation et Adaptation de Raffinerie de Skikda”. 
Dans le cadre de “Projet de Réhabilitation et Adaptation” de la Raffinerie de Skikda, certaines unités ont été modernisées et quelques nouvelles unités ont été ajoutées.

El siguiente trabajo presentado ante la Universidad Nacional San Martin de la Argentina (UNSAM) – Instituto Petroquímico Argentino (IPA), para optar el Título de ESPECIALISTA EN INDUSTRIA PETROQUIMICA, muestra la viabilidad técnico-económica de la instalación de una planta de producción de Policloruro de Vinilo (PVC) en la Región Arequipa, localizada a 1,000 km al sur de Lima – Perú.
El Estado Peruano desde el año 2006 viene dando el Marco Legal y normativo para promover la Industria Petroquímica en el Perú (Ley Nro. 29163 de Promoción de la Petroquímica) a partir del Gas Natural de Camisea.
Inicialmente por cercanía al ducto de Transportadora de Gas del Perú (TGP) que trae el GN desde Camisea a la costa de Lima (Melchorita), se plantearon proyectos petroquímicos como el de Nitratos del Perú (grupos mineros Sigdo Koppers – Brescia US$ 850 MM en ciudad de Pisco – Ica a +/-100 km), CF Industries (Marcona-Ica US$ 2,000 MM, urea y amoniaco para fertilizantes), ORICA que planteo relocalizarse de Ica a Ilo.
Todos estos proyectos quedaron de lado por la Concesión otorgada (2008) para la construcción del Gasoducto Sur Andino de KUNTUR el mismo que requería demanda de GN al final del ducto en Arequipa – Ilo; y por la dación de la Ley Nro. 29690 que promueve y determina que la petroquímica del Etano solo podrá instalarse en el Sur del Perú (2011) y que obligatoriamente se deberá separar el etano del gas de Camisea para abastecer un cracker y obtener etileno para el Polo Petroquímico Descentralizado del Sur.
La decisión política de llevar la Petroquímica al Sur adoptada por el Presidente A. García (Julio 2006 – Julio 2011) se basó en qué; si bien la zona sur del Perú es la zona más excluida, postergada y de menor desarrollo; esta cuenta con infraestructura portuaria, vías de comunicación, energía, universidades, aeropuertos y otros.
Con la dación de la Ley Nro. 29970 de Afianzamiento de la Seguridad Energética y Desarrollo del Polo Petroquímico en el Sur del Perú (2013) y Resolución Suprema Nro. 005-2013-EF, que permitió que PROINVERSION convocara y adjudicara la construcción del Gasoducto Sur Peruano (GSP) conformado por Odebrecht – Enagas – Graña Montero.
Creciendo a un CAGR del 5.0%, se espera que el mercado mundial de PVC llegue a US$ 79.11 mil millones para el 2020 debido al aumento del gasto en construcción e infraestructura en los mercados emergentes de Asia Pacífico. Y América Latina siga siendo un factor clave para la demanda global de PVC.
Se viene desarrollando desde muchos años atrás los estudios para la instalación de un cracker de etileno de 1000 kta, y aquí para tal capacidad instalada se propone se produciría 840.4 kta de etileno para producir polietilenos y 159.6 kta de etileno para producir 350 kta de PVC, en una planta cercana a un proyecto minero que tiene como subproducto salmuera, materia prima requerida para instalar una Planta Cloro álcali, para producir PVC.
Se presenta el estudio económico para la instalación de una PLANTA CLORO ÁLCALI de 204,000 TMA, una planta de producción de VCM y PVC ambas con una capacidad de 350,000 TMA; este proyecto requerirá de una inversión de 1,001 millones de dólares.
El proyecto es rentable de acuerdo a la evaluación económica, a una tasa de interés del 12% el VAN es de 205.29 millones de dólares y un TIR de 13.77% demostrando la rentabilidad del proyecto sumado a un tiempo de recuperación de la inversión de 5.29 años.

Las estrictas normas ambientales han incrementado el costo de producir combustibles limpios. Esto motivó la búsqueda para producir combustibles limpios por métodos no convencionales. La alquilación de olefinas y la síntesis de Fisher-Tropsch son otros posibles métodos para producir combustibles limpios. La nueva tecnología y el mejor diseño de equipos de refinería también está siendo desarrollado con el fin de producir combustibles más limpios y baratos.

The purpose of this paper is to indicate the problems and deficiencies in current practice in our country for the design of industrial structures, specifically in the field of hydrocarbons, which results from using current codes and standards as MDOC CFE-2008 and the unsupported combination with international codes such as ASCE 7-10, ACI 318-11 and AISC 325-11, which is caused as a contractual obligation that has so far been inevitable. The consequence of such a fusion of philosophies can cause deficient and expensive designs, or with a level of security difficult to assess due to the high uncertainty in various parameters and factors involved in the design.

Amine Gas Treating Unit  - Best Practices - Troubleshooting Guide for H2S/CO2 Amine Systems
Contents
Process Capabilities for gas treating process
Typical Amine Treating
Typical Amine System Improvements
Primary Equipment Overview
Inlet Gas Knockout
Absorber
Three Phase Flash Tank
Lean/Rich Heat Exchanger
Regenerator
Filtration
Amine Reclaimer
Operating Difficulties Overview
Foaming
Failure to Meet Gas Specification
Solvent Losses
Corrosion
Typical Amine System Improvements
Degradation of Amines and Alkanolamines during Sour Gas Treating
APPENDIX
Best Practices - Troubleshooting Guide

Many smart Petrochemical engineers fail to get good jobs because  they don't succeed in interviews.
Why?
They never respond meaningfully and convincingly on the spot.
Why?
Two reasons: First, their preparation involves only 'technical topics'. Second, they are not aware of their own talking style and likeability.
This brochure is about world's first Petrochemical Engineering Interview Simulator & Trainer. It provides infinite number of mock interviews with recording and training features.

Shift Conversion Catalysts:  Operating Manual
Contents
Introduction
High temperature shift catalysts
Low temperature shift catalysts
Catalyst storage, handling, charging and discharging
Health and safety precautions
Reduction and start-up of high temperature shift catalysts
Operation of high temperature shift catalysts
Reduction and start-up of low temperature shift catalysts
Operation of low temperature shift catalysts

Sulfiding of Sour Shift Catalyst
Introduction to Sour Shift Catalysts VIG SGS-201/202/203
Feedstock's from the gasification of coal or heavy oil contain high levels of sulfur.
Conventional iron-chrome catalysts are not suitable
“Sour” or “Dirty” shift catalysts were developed.
These catalysts achieve maximum activity in the sulfided state.
Require treatment with Sulfur prior to start-up.
Can only be used in streams that contain sufficient sulfur to maintain them in this state

Artificial lift methods are used for the enhancement of productivity from oil wells. These methods are implemented in oil wells whose energy from the reservoir is insufficient to lift the fluids to the surface. In this study about Electrical submersible pump and its design & simulation in PROSPER software. It is one of the important type of artificial lift methods, which is used to lower the producing bottom hole pressure on the formation to obtain a higher production rate from the well. It is an efficient and reliable method for lifting moderate to high volumes of fluids from wellbores. PROSPER is a well performance, design and optimization computer software for modelling most types of well configurations. This study major focuses on the design and simulation of an ESP system for wells having different productivity index using the PROSPER software.

Pada laporan tugas khusus kerja praktik di PT. Mitsubishi Chemical Indoensia ini bertujuan untuk menganalisa koefisien perpindahan panas pada kondensor saat sebelum dan sesudah blackout dan menganalisa pengaruh clogging terhadap koefisien perpindahan panas pada kondensor dan menghitung kerugian akibat dari clogging.

Pressure Relief Systems
Causes of Relief Situations Vol.2 of 6

This Volume 2,  is a guide to the qualitative identification of common causes of overpressure in process equipment. It cannot be exhaustive; the process engineer and relief systems team should look for any credible situation in addition to those given in this Part which could lead to a need for pressure relief (a relief situation).

Pressure Relief Systems
BACKGROUND TO RELIEF SYSTEM DESIGN Vol.1 of 6

The Guide has been written to advise those involved in the design and engineering of pressure relief systems. It takes the user from the initial identification of potential causes of overpressure or under pressure through the process design of relief systems to the detailed mechanical design. "Hazard Studies" and quantitative hazards analysis are not described; these are seen as complementary activities. Typical users of the Guide will use some Parts in detail and others in overview

Adiabatic Reactor Analysis for Methanol Synthesis 
Plant Note Book Series: PNBS-0604
Contents
I. Energy Balance and the Conversion-Temperature Relationship
II. Mass Balance and Rate Expression
III. Inlet Conditions
IV.A. Calculation 1: Solve for 5% conversion (X = 0.05)
IV.B. Calculation 2: Solve for 10% conversion (X = 0.10)
IV.C. Calculation 3: Solve for 50% Conversion (X = 0.50)
IV.D. Generate Data for Levenspiel Plot

Theory of Carbon Formation in Steam Reforming
Contents
1 Introduction
2 Underpinning Theory
2.1 Conceptualization
2.2 Reforming Reactions
2.3 Carbon Formation Chemistry
2.3.1 Natural Gas
2.3.2 Carbon Formation for Naphtha Feeds
2.3.3 Carbon Gasification
2.4 Heat Transfer
3 Causes
3.1 Effects of Carbon Formation
3.2 Types of Carbon
4 What are the Effects of Carbon Formation?
4.1 Why does Carbon Formation Get Worse?
4.1.1So what is the Next Step?
4.2 Consequences of Carbon Formation
4.3 Why does Carbon Form where it does?
4.3.1Effect on Process Gas Temperature
4.4 Why does Carbon Formation Propagate Down the Tube?
4.4.1 Effect on Radiation on the Fluegas Side
4.5 Why does Carbon Formation propagate Up the Tube?
5 How do we Prevent Carbon Formation
5.1 The Role of Potash
5.2 Inclusion of Pre-reformer
5.3 Primary Reformer Catalyst Parameters
5.3.1 Activity
5.3.2 Heat Transfer
5.3.3 Increased Steam to Carbon Ratio
6 Steam Out
6.1 Why does increasing the Steam to Carbon Ratio Not Work?
6.2 Why does reducing the Feed Rate not help?
6.3 Fundamental Principles of Steam Outs

TABLES
1 Heat Transfer Coefficients in a Typical Reformer
2 Typical Catalyst Loading Options

FIGURES
1 Hot Bands
2 Conceptual Pellet
3 Naphtha Carbon Formation
4 Heat Transfer within an Reformer
5 Types of Carbon Formation
6 Effect of Carbon on Nickel Crystallites
7 Absorption of Heat
8 Comparison of  "Base Case" v Carbon Forming Tube
9 Carbon Formation Vicious Circle
10 Temperature Profiles
11 Carbon Pinch Point
12 Carbon Formation
13 Effect on Process Gas Temperature
14 How does Carbon Propagate into an Unaffected Zone?
15 Movement of the Carbon Forming Region
16 Effect of Hot Bands on Radiative Heat Transfer
17 Effect of Potash on Carbon Formation
18 Application of a Pre-reformer
19 Effect of Activity on Carbon Formation

DESIGN OF VENT GAS COLLECTION AND DESTRUCTION SYSTEMS
CONTENTS
1 INTRODUCTION
1.1 Purpose
1.2 Scope of this Guide
1.3 Use of the Guide
2 ENVIRONMENTAL ISSUES
2.1 Principal Concerns
2.2 Mechanisms for Ozone Formation
2.3 Photochemical Ozone Creation Potential
2.4 Health and Environmental Effects
2.5 Air Quality Standards for Ground Level Concentrations of Ozone, Targets for Reduction of VOC Discharges and Statutory Discharge Limits
3 VENTS REDUCTION PHILOSOPHY
3.1 Reduction at Source
3.2 End-of-pipe Treatment
4 METHODOLOGY FOR COLLECTION & ASSESSMENT OF PROCESS FLOW DATA
4.1 General
4.2 Identification of Vent Sources
4.3 Characterization of Vents
4.4 Quantification of Process Vent Flows
4.5 Component Flammability Data Collection
4.6 Identification of Operating Scenarios
4.7 Quantification of Flammability Characteristics for Combined Vents
4.8 Identification, Quantification and Assessment of Possibility of Air Ingress Routes
4.9 Tabulation of Data
4.10 Hazard Study and Risk Assessment
4.11 Note on Aqueous / Organic Wastes
4.12 Complexity of Systems
4.13 Summary
5 SAFE DESIGN OF VENT COLLECTION HEADER SYSTEMS
5.1 General
5.2 Process Design of Vent Headers
5.3 Liquid in Vent Headers
5.4 Materials of Construction
5.5 Static Electricity Hazard
5.6 Diversion Systems
5.7 Snuffing Systems
6 SAFE DESIGN OF THERMAL OXIDISERS
6.1 Introduction
6.2 Design Basis
6.3 Types of High Temperature Thermal Oxidizer
6.4 Refractories
6.5 Flue Gas Treatment
6.6 Control and Safety Systems
6.7 Project Program
6.8 Commissioning
6.9 Operational and Maintenance Management
APPENDICES
A GLOSSARY
B FLAMMABILITY
C EXAMPLE PROFORMA
D REFERENCES

DOCUMENTS REFERRED TO IN THIS PROCESS GUIDE

TABLE

1 PHOTOCHEMICAL OZONE CREATION POTENTIAL REFERENCED
TO ETHYLENE AS UNITY


FIGURES

1 SCHEMATIC OF TYPICAL VENT COLLECTION AND THERMAL OXIDIZER SYSTEM
2 TYPICAL KNOCK-OUT POT WITH LUTED DRAIN
3 SCHEMATIC OF DIVERSION SYSTEM
4 CONVENTIONAL VERTICAL THERMAL OXIDIZER
5 CONVENTIONAL OXIDIZER WITH INTEGRAL WATER SPARGER
6 THERMAL OXIDIZER WITH STAGED AIR INJECTION
7 DOWN-FIRED UNIT WITH WATER BATH QUENCH
8 FLAMELESS THERMAL OXIDATION UNIT
9 THERMAL OXIDIZER WITH REGENERATIVE HEAT RECOVERY
10 TYPICAL PROJECT PROGRAM
11 TYPICAL FLAMMABILITY DIAGRAM
12 EFFECT OF DILUTION WITH AIR
13 EFFECT OF DILUTION WITH AIR ON 100 Rm³ OF FLAMMABLE GAS

PRACTICAL GUIDE TO DEVELOPING PROCESS FLOW DIAGRAMS AND  PRELIMINARY ENGINEERING LINE DIAGRAMS PROCESS
CONTENTS

1 INTRODUCTION

2 DESCRIPTION OF METHODOLOGY
2.1 Philosophy of the Design Process
2.2 Outline of Methodology
2.3 Additional Aspects of Methodology

3 WORKBOOK

4  EXAMPLE: BATCH NEUTRALIZATION AND STRIPPING PROCESS
4.1 Start of Stage 1
4.2 Stage 1
4.3 Stage 2
4.3 Stage 3

5 REFERENCES

TABLES
1 DESIGN OBJECTIVES
2 OUTPUT FROM EACH STAGE
3 STEP BY STEP APPROACH
4 FUNCTION
5 OPERATION
6 FAILURES
7 STAGE 3 PROMPTS (DATA SHEET)
8 PRELIMINARY MASS BALANCE
9 PRELIMINARY EQUIPMENT LIST
10 POTENTIAL PROBLEMS
11 STAGE 2: DEVELOPMENT OF OPERATING STATES AND TRANSMISSIONS
12 POTENTIAL PROBLEMS

FIGURES
1 DESIGN PROCESS
2 DESIGN PHILOSOPHY.
3 SUMMARY OF METHODOLOGY
4 POSSIBLE OUTCOMES FROM A KEYWORD PROMPT
5 OPERATING STATES
6 OPERATING STATES/TRANSITIONS
7 EXAMPLE: OVERALL BLOCK DIAGRAM
8 EXAMPLE: “PRIMITIVE PFD”
9 EXAMPLE: STAGE 1 “WORKING DIAGRAM”.
10 EXAMPLE: MAIN OPERATING STATES AND TRANSITIONS
11 EXAMPLE: DETAILED PFD (END OF STAGE 1)
12 EXAMPLE: STAGE 2 “WORKING DIAGRAM”
13 EXAMPLE: STAGE 3 “REV 0” ELD