Amine Gas Treating Unit - Best Practices - Troubleshooting Guide Gerard B. Hawkins
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
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
This is a full course about how the Amine Sweetening Unit works, and all the factors, operations, and problems related to this unit. This course was taken from the IHRDC institute.
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
This program addresses in an integrated manner the key activities involved in the safe, effective and timely commissioning and start-up of a new plant or facility. Start Up and Commissioning of new plant and equipment presents both a major technical and management challenge. An organisation’s personnel must familiarise themselves with new equipment, processes and technologies, develop the relevant operating and safety procedures.
At the same time there is the requirement to execute an exceptionally large scope of work – much of it complex when compared to routine operations - over a short period of time, with equipment and plant which is as yet unproven and that may pose significant risks to personnel, environment and profitability.
This 5 day training course addresses the technical issues of commissioning and starting up various equipment and asset types commonly found in processing plant environments, the development of specific commissioning procedures, process and facility wide commissioning strategies. The course will also address the broader managerial issues of commissioning and start up planning, resourcing, budgeting and cost control, risk management – safety, environmental, financial and operational, problem solving and trouble shooting.
Amine Gas Treating Unit - Best Practices - Troubleshooting Guide Gerard B. Hawkins
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
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
This is a full course about how the Amine Sweetening Unit works, and all the factors, operations, and problems related to this unit. This course was taken from the IHRDC institute.
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
This program addresses in an integrated manner the key activities involved in the safe, effective and timely commissioning and start-up of a new plant or facility. Start Up and Commissioning of new plant and equipment presents both a major technical and management challenge. An organisation’s personnel must familiarise themselves with new equipment, processes and technologies, develop the relevant operating and safety procedures.
At the same time there is the requirement to execute an exceptionally large scope of work – much of it complex when compared to routine operations - over a short period of time, with equipment and plant which is as yet unproven and that may pose significant risks to personnel, environment and profitability.
This 5 day training course addresses the technical issues of commissioning and starting up various equipment and asset types commonly found in processing plant environments, the development of specific commissioning procedures, process and facility wide commissioning strategies. The course will also address the broader managerial issues of commissioning and start up planning, resourcing, budgeting and cost control, risk management – safety, environmental, financial and operational, problem solving and trouble shooting.
Methanol Casale Advanced Reactor Concept (ARC) Converter Retrofit CASE STUDY #10231406
For older methanol plants, efficiency is worse than for a modern plant
• To maximize profit we must improve either
– Plant efficiency
– Plant production rate
This case study highlights the revamp of a Middle Eastern Methanol Plant ARC converter with part IMC internals, to improve efficiency and production; with no CO2 addition to the Synloop, and with CO2 addition to the Synloop.
- 250 TPD CO2
- 500 TPD CO2
Natural Gas (from a natural reservoir or associated to a crude production) can contain acid gas (H2S and/or CO2)..
The Gas Sweetening Process aims to remove part or all of the acid gas.
Reactor Arrangement for Continuous Vapor Phase ChlorinationGerard B. Hawkins
Reactor Arrangement for Continuous Vapor Phase Chlorination
CONTENTS
1 BACKGROUND
2 REACTOR
3 CHEMICAL SYSTEM
4 PROCESS CHEMISTRY
5 KINETICS EXPERIMENTS AND MODELING
6 INTERPRETATION OF KINETICS INFORMATION
7 OPERATING CONDITIONS AND REACTOR DESIGN
8 REACTOR STABILITY AND CONTROL
FIGURES
1 POSTULATED REACTION PATHS FOR PROGRESSIVE CHLORINATION OF B-PICOLINE 3
2 CHLORINATION OF b-PICOLINE: MODEL PREDICTIONS OF PRODUCT DISTRIBUTION IN FULLY-MIXED REACTOR
3 TWO-STAGE REACTOR: RATE OF CHLORINATION OF b-PICOLINE
DOCUMENTS REFERRED TO IN THIS PROCESS ENGINEERING GUIDE
VULCAN Series VSG-Z101 Primary Reforming
Initial Catalyst Reduction
Activating (reducing) the catalyst involves changing the nickel oxide to nickel, represented by:
NiO + H2 <==========> Ni + H2O
Natural gas is typically used as the hydrogen source. When it is, the catalyst reduction and putting the reformer on-line are accompanied in the same step.
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.
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”
The explosion hazard in urea process (1)Prem Baboo
In Urea plant passivation air is used in reactor, stripper and downstream of the all equipments. The reactor liner material used Titanium, Zirconium, SS 316L (urea grade), 2RE-69 and duplex material .except Titanium and Zirconium all stainless steel required more passivation air. In CO2 some quantity of Hydrogen is present about 0.14% to 0.2% . The passivation oxygen and Hydrogen makes explosive mixture. To avoid a fire or explosion in a process vessel is to introduce inert (noncombustible) gases in such a way that there is never a mixture with a combustible concentration in exit of MP vent. Mixtures of fuel, oxygen, and inert gases are not combustible over the entire range of composition. In CO2 stripping process the HP scrubber is the risky vessel and this vessel consisting blanketing sphere, Heat exchanger part and a scrubbing part. With help of triangular diagram that shows the shape of the combustible/noncombustible regions for a typical gaseous mixture of fuel, oxygen, and inert at specified temperature and pressure. Present article how to avoid that combustible rang and how to tackle that gases in CO2 & ammonia stripping process.
Ammonia Plant Technology
Pre-Commissioning Best Practices
GBHE-APT-0102
PICKLING & PASSIVATION
CONTENTS
1 PURPOSE OF THE WORK
2 CHEMICAL CONCEPT
3 TECHNICAL CONCEPT
4 WASTES & SAFETY CONCEPT
5 TARGET RESULTS
6 THE GENERAL CLEANING SEQUENCE MANAGEMENT
6.6.1 Pre-cleaning or “Physical Cleaning
6.6.2 Pre-rinsing
6.6.3 Chemical Cleaning
6.6.4 Critical Factors in Cleaning Success
6.6.5 Rinsing
6.6.6 Inspection and Re-Cleaning, if Necessary
7 Systems to be treated by Pickling/Passivation
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?
4.1.1 So what is the Next Step?
4.2 Consequences of Carbon Formation
4.3 Why does Carbon Form where it does?
4.3.1 Effect 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
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
ACETYLENE SAFETY & ACETYLENE PROCESS HAZARDSHashim Badat
Initially, this presentation was prepared and used as a training tool for Engineers and Process Technicians who worked on the Chemical process where acetylene was used as one of the raw materials. However, for the purpose of sharing it on this forum, it has been modified to include additional sections e.g. Basic chemistry, Acetylene manufacturing, etc.
Starting PA Fans, Taking Coal Mills in service, Charging LP Heaters, Taking second BFP in service, Charging HP Heaters, UPS fast bus Transfer scheme, Loading to full load 210 MW
Top 10 “Must Do's” for Implementing an Assessment Process in Your ProgramExamSoft
Dr. Kyumin Whang, Associate Professor, The University of Texas Health Science Center at San Antonio, School of Dentistry
Implementation of a new technology in an educational program is never an easy feat. On-boarding and receiving faculty buy-in can be challenging, but with careful planning is achievable. This presentation will share The University of Texas Health Science Center at San Antonio (UTHSCSA) School of Dentistry’s best practices for implementation, set-up, and construction of assessment procedure to ensure successful adoption and continued use of ExamSoft. Topics covered will include: advantages and challenges of implementation, collaboration with specialists and technicians, setup of support systems, and construction of student academic misconduct procedures.
Methanol Casale Advanced Reactor Concept (ARC) Converter Retrofit CASE STUDY #10231406
For older methanol plants, efficiency is worse than for a modern plant
• To maximize profit we must improve either
– Plant efficiency
– Plant production rate
This case study highlights the revamp of a Middle Eastern Methanol Plant ARC converter with part IMC internals, to improve efficiency and production; with no CO2 addition to the Synloop, and with CO2 addition to the Synloop.
- 250 TPD CO2
- 500 TPD CO2
Natural Gas (from a natural reservoir or associated to a crude production) can contain acid gas (H2S and/or CO2)..
The Gas Sweetening Process aims to remove part or all of the acid gas.
Reactor Arrangement for Continuous Vapor Phase ChlorinationGerard B. Hawkins
Reactor Arrangement for Continuous Vapor Phase Chlorination
CONTENTS
1 BACKGROUND
2 REACTOR
3 CHEMICAL SYSTEM
4 PROCESS CHEMISTRY
5 KINETICS EXPERIMENTS AND MODELING
6 INTERPRETATION OF KINETICS INFORMATION
7 OPERATING CONDITIONS AND REACTOR DESIGN
8 REACTOR STABILITY AND CONTROL
FIGURES
1 POSTULATED REACTION PATHS FOR PROGRESSIVE CHLORINATION OF B-PICOLINE 3
2 CHLORINATION OF b-PICOLINE: MODEL PREDICTIONS OF PRODUCT DISTRIBUTION IN FULLY-MIXED REACTOR
3 TWO-STAGE REACTOR: RATE OF CHLORINATION OF b-PICOLINE
DOCUMENTS REFERRED TO IN THIS PROCESS ENGINEERING GUIDE
VULCAN Series VSG-Z101 Primary Reforming
Initial Catalyst Reduction
Activating (reducing) the catalyst involves changing the nickel oxide to nickel, represented by:
NiO + H2 <==========> Ni + H2O
Natural gas is typically used as the hydrogen source. When it is, the catalyst reduction and putting the reformer on-line are accompanied in the same step.
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.
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”
The explosion hazard in urea process (1)Prem Baboo
In Urea plant passivation air is used in reactor, stripper and downstream of the all equipments. The reactor liner material used Titanium, Zirconium, SS 316L (urea grade), 2RE-69 and duplex material .except Titanium and Zirconium all stainless steel required more passivation air. In CO2 some quantity of Hydrogen is present about 0.14% to 0.2% . The passivation oxygen and Hydrogen makes explosive mixture. To avoid a fire or explosion in a process vessel is to introduce inert (noncombustible) gases in such a way that there is never a mixture with a combustible concentration in exit of MP vent. Mixtures of fuel, oxygen, and inert gases are not combustible over the entire range of composition. In CO2 stripping process the HP scrubber is the risky vessel and this vessel consisting blanketing sphere, Heat exchanger part and a scrubbing part. With help of triangular diagram that shows the shape of the combustible/noncombustible regions for a typical gaseous mixture of fuel, oxygen, and inert at specified temperature and pressure. Present article how to avoid that combustible rang and how to tackle that gases in CO2 & ammonia stripping process.
Ammonia Plant Technology
Pre-Commissioning Best Practices
GBHE-APT-0102
PICKLING & PASSIVATION
CONTENTS
1 PURPOSE OF THE WORK
2 CHEMICAL CONCEPT
3 TECHNICAL CONCEPT
4 WASTES & SAFETY CONCEPT
5 TARGET RESULTS
6 THE GENERAL CLEANING SEQUENCE MANAGEMENT
6.6.1 Pre-cleaning or “Physical Cleaning
6.6.2 Pre-rinsing
6.6.3 Chemical Cleaning
6.6.4 Critical Factors in Cleaning Success
6.6.5 Rinsing
6.6.6 Inspection and Re-Cleaning, if Necessary
7 Systems to be treated by Pickling/Passivation
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?
4.1.1 So what is the Next Step?
4.2 Consequences of Carbon Formation
4.3 Why does Carbon Form where it does?
4.3.1 Effect 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
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
ACETYLENE SAFETY & ACETYLENE PROCESS HAZARDSHashim Badat
Initially, this presentation was prepared and used as a training tool for Engineers and Process Technicians who worked on the Chemical process where acetylene was used as one of the raw materials. However, for the purpose of sharing it on this forum, it has been modified to include additional sections e.g. Basic chemistry, Acetylene manufacturing, etc.
Starting PA Fans, Taking Coal Mills in service, Charging LP Heaters, Taking second BFP in service, Charging HP Heaters, UPS fast bus Transfer scheme, Loading to full load 210 MW
Top 10 “Must Do's” for Implementing an Assessment Process in Your ProgramExamSoft
Dr. Kyumin Whang, Associate Professor, The University of Texas Health Science Center at San Antonio, School of Dentistry
Implementation of a new technology in an educational program is never an easy feat. On-boarding and receiving faculty buy-in can be challenging, but with careful planning is achievable. This presentation will share The University of Texas Health Science Center at San Antonio (UTHSCSA) School of Dentistry’s best practices for implementation, set-up, and construction of assessment procedure to ensure successful adoption and continued use of ExamSoft. Topics covered will include: advantages and challenges of implementation, collaboration with specialists and technicians, setup of support systems, and construction of student academic misconduct procedures.
Atlas Industries manufacturer of world class Road & Civil Construction Equipments. Atlas company strongly believes in quality & considered specialized in prompt delivery.
Back 2 basics - LEARNING FROM ACCIDENTS - No more missed opportunities - A Tr...Manuel Rodríguez Herrán
Presentation including some basic ideas, not always taken into account, about some accident investigation clichés and the importance of using and disseminating information obtained from the accidents already happened, in order to avoid they become missed opportunities to prevent similar situations. All based on the Trevor Kletz's legacy. Expounded in Antwerpen (Belgium) on October 27, 2016 (DEKRA Insight 'Safety in Action' Conference) and in Madrid on Novemeber 17, 2016 (IRSST Technical Session 'The accidents investigation as a preventative improvement tool'). The presentation includes some more quotes and a bonus slide, not expounded in Antwerpen.
5 Tips for Creating Standard Financial ReportsEasyReports
Well-crafted financial reports serve as vital tools for decision-making and transparency within an organization. By following the undermentioned tips, you can create standardized financial reports that effectively communicate your company's financial health and performance to stakeholders.
2. Elemental Economics - Mineral demand.pdfNeal Brewster
After this second you should be able to: Explain the main determinants of demand for any mineral product, and their relative importance; recognise and explain how demand for any product is likely to change with economic activity; recognise and explain the roles of technology and relative prices in influencing demand; be able to explain the differences between the rates of growth of demand for different products.
how to sell pi coins in South Korea profitably.DOT TECH
Yes. You can sell your pi network coins in South Korea or any other country, by finding a verified pi merchant
What is a verified pi merchant?
Since pi network is not launched yet on any exchange, the only way you can sell pi coins is by selling to a verified pi merchant, and this is because pi network is not launched yet on any exchange and no pre-sale or ico offerings Is done on pi.
Since there is no pre-sale, the only way exchanges can get pi is by buying from miners. So a pi merchant facilitates these transactions by acting as a bridge for both transactions.
How can i find a pi vendor/merchant?
Well for those who haven't traded with a pi merchant or who don't already have one. I will leave the telegram id of my personal pi merchant who i trade pi with.
Tele gram: @Pi_vendor_247
#pi #sell #nigeria #pinetwork #picoins #sellpi #Nigerian #tradepi #pinetworkcoins #sellmypi
how to sell pi coins effectively (from 50 - 100k pi)DOT TECH
Anywhere in the world, including Africa, America, and Europe, you can sell Pi Network Coins online and receive cash through online payment options.
Pi has not yet been launched on any exchange because we are currently using the confined Mainnet. The planned launch date for Pi is June 28, 2026.
Reselling to investors who want to hold until the mainnet launch in 2026 is currently the sole way to sell.
Consequently, right now. All you need to do is select the right pi network provider.
Who is a pi merchant?
An individual who buys coins from miners on the pi network and resells them to investors hoping to hang onto them until the mainnet is launched is known as a pi merchant.
debuts.
I'll provide you the Telegram username
@Pi_vendor_247
This presentation poster infographic delves into the multifaceted impacts of globalization through the lens of Nike, a prominent global brand. It explores how globalization has reshaped Nike's supply chain, marketing strategies, and cultural influence worldwide, examining both the benefits and challenges associated with its global expansion.
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Nike Supply Chain
Globalization of Nike
Nike Manufacturing Process
Rubber Materials Nike
Ethylene Vinyl Acetate Nike
Genuine Leather Nike
Synthetic Leather Nike
Cotton in Nike Apparel
Nike Shops Worldwide
Nike Manufacturing Countries
Cold Cement Assembly Nike
3D Printing Nike Shoes
Nike Product Development
Nike Marketing Strategies
Nike Customer Feedback
Nike Distribution Centers
Automation in Nike Manufacturing
Nike Consumer Direct Acceleration
Nike Logistics and Transport
Turin Startup Ecosystem 2024 - Ricerca sulle Startup e il Sistema dell'Innov...Quotidiano Piemontese
Turin Startup Ecosystem 2024
Una ricerca de il Club degli Investitori, in collaborazione con ToTeM Torino Tech Map e con il supporto della ESCP Business School e di Growth Capital
BYD SWOT Analysis and In-Depth Insights 2024.pptxmikemetalprod
Indepth analysis of the BYD 2024
BYD (Build Your Dreams) is a Chinese automaker and battery manufacturer that has snowballed over the past two decades to become a significant player in electric vehicles and global clean energy technology.
This SWOT analysis examines BYD's strengths, weaknesses, opportunities, and threats as it competes in the fast-changing automotive and energy storage industries.
Founded in 1995 and headquartered in Shenzhen, BYD started as a battery company before expanding into automobiles in the early 2000s.
Initially manufacturing gasoline-powered vehicles, BYD focused on plug-in hybrid and fully electric vehicles, leveraging its expertise in battery technology.
Today, BYD is the world’s largest electric vehicle manufacturer, delivering over 1.2 million electric cars globally. The company also produces electric buses, trucks, forklifts, and rail transit.
On the energy side, BYD is a major supplier of rechargeable batteries for cell phones, laptops, electric vehicles, and energy storage systems.
3. Jonathan Stuart
Vice President
Regional Refinery Operations
3
4. Crude Oil Characteristics
Crudes are classified and priced by density and sulfur content
Crude density is commonly measured by API gravity
• API gravity provides a relative measure of crude oil density
• The higher the API number, the lighter the crude
− Light crudes are easier to process
− Heavy crudes are more difficult to process
Crude sulfur content is measured as a percentage
• Less than 0.7% sulfur content = sweet
• Greater than 0.7% sulfur content = sour
• High sulfur crudes require additional processing to meet regulatory specs
Acid content is measured by Total Acid Number (TAN)
• Acidic crudes highly corrosive to refinery equipment
• High acid crudes are those with TAN greater than 0.7
4
5. Crude Oil Basics
Crude Quality by Types Estimated Quality of Reserves (2006)
4.0%
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Cerro Negro
3.5%
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3.0%
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Arab Heavy
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2010 13%
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1990
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1.0%
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1980
0.5% WTI
Brent
Tapis
Cabinda Bonny Light
0.0%
15 20 25 30 35 40 45 50
Source: Oil & Gas Journal, Company Information
HEAVY API GRAVITY LIGHT
Source: Industry reports
NOTE: Red line represents the average crude quality by decade (actual and projected)
Majority of global reserves are sour
Most quoted benchmark prices are light sweet crudes
• WTI (West Texas Intermediate), Western Hemisphere
• Brent (North Sea Crude), Europe
Historical trend shows global crude supply becoming heavier and more sour
5
6. What’s in a Barrel of Crude Oil?
Crude Types Characteristics Yields
2005 U.S.
3%
Production
> 34 API Gravity
30%
Light Sweet Crude < 0.7 % Sulfur
Propane/
(e.g. WTI, Brent, Saharan Refinery
8%
34% Butane
7% Gases
35% Demand
Blend)
33%
Most Expensive
Gasoline
RFG
50% Conventional
3% CARB
24 – 34 API Gravity Premium
21%
Medium Sour Crude > 0.7 % Sulfur
(e.g. Mars, Arab Light, 26%
Arab Medium, Urals) 50% Demand
Distillate
33%
50%
Jet Fuel
Less Expensive
Diesel
Heating Oil
1%
< 24 API Gravity
14%
Heavy
10%
> 0.7 % Sulfur Fuel Oil &
22%
Heavy Sour Crude Other
15% Demand
(e.g. Maya, Cerro Negro, Cold
Lake, Western Canadian Select) Source: EIA Refiner Production
63%
Least Expensive
Refineries upgrade crude oil to higher value products
6
7. Basic Refining Concepts
Intermediates Final Products
< 90°F Propane, Butane • Refinery fuel gas
and lighter • Propane
• NGLs
Straight Run
90–220°F More
• Gasoline (high octane)
Gasoline (low
processing
octane)
Crude oil
More
220–315°F • Gasoline (high octane)
Naphtha
• Jet fuel
Distillation processing
Tower
• Kerosene
(Crude
More
315–450°F • Jet fuel
Unit) Kerosene
• Diesel
processing
• Fuel oil
• Gasoline (high octane)
More
450–650°F Light Gas Oil • Diesel
Furnace processing
• Fuel oil
• Gasoline (high octane)
More
650–800°F Heavy Gas Oil • Diesel
Vacuum processing • Fuel oil
Unit
• Gasoline (high octane)
Residual Fuel More
800+°F • Diesel
Oil/Asphalt • Fuel oil
processing
• Lube stocks
7
8. Hydroskimming/Topping Refinery
Crude
Unit
Propane/
4%
Propane/Butane
Butane
Gasoline
Reformer High Octane Gasoline
Low Octane Gasoline RFG
Distillation Tower
30%
and Naphtha Conventional
CARB
Hydrogen
Premium
Light
Distillate
HS Kerosene/Jet Fuel
Sweet LS Kerosene/Jet Fuel
Distillate
34%
Desulfurizer
Jet Fuel
Crude Diesel
LS Diesel/Heating Oil
HS Diesel/Heating Oil
Heating Oil
Heavy
Gas Oil
Vacuum Fuel Oil &
32%
Unit Other
Heavy Fuel Oil
100% Total Yield
Simple, low upgrading capability refineries run sweet crude
8
10. Medium Conversion: Catalytic
Cracking
Crude
Propane/
Unit
8% Butane
Propane/Butane
Gasoline
RFG
Reformer High Octane Gasoline
Low Octane Gasoline 45% Conventional
and Naphtha
Distillation Tower
CARB
Premium
Hydrogen
Distillate
Light LS Kerosene/Jet Fuel
HS Kerosene/Jet Fuel
Desulfurizer Distillate
27%
Sour Jet Fuel
HS Diesel/Heating Oil LS Diesel/Heating Oil Diesel
Crude Heating Oil
Light Cycle Oil
(LCO)
Alkylation
Alkylate
Unit
Fluid Catalytic
Gas Oil
Vacuum Cracker
Unit FCC Gasoline
(FCC) Heavy
Fuel Oil &
24% Other
Heavy Fuel Oil
104% Total Yield
Moderate upgrading capability refineries tend to run more sour crudes
while achieving increased higher value product yields and volume gain
10
11. High Conversion: Coking/Resid
Destruction
Hydrogen Plant
Crude
Gas
Unit
Propane/
7% Butane
Propane/Butane
Gasoline
RFG
Distillation Tower
58%
Reformer High Octane Gasoline Conventional
Low Octane Gasoline
CARB
and Naphtha
Medium/ Premium
Hydrogen
Heavy Distillate
Distillate 28%
HS Kerosene/Jet Fuel LS Kerosene/Jet Fuel
Sour Desulfurizer Jet Fuel
Diesel
Crude Heating Oil
LS Diesel/Heating Oil
HS Diesel/Heating Oil
Hydrocracker Hydrocrackate Gasoline
Light Gas Oil
Ultra Low Sulfur Jet/Diesel
LCO Alkylation
Alky Gasoline
Unit
Fluid Catalytic
Cracker (FCC)
Medium Gas Oil
Vacuum
FCC Gasoline
Unit
Heavy
Fuel Oil &
15% Other
Delayed
Heavy Fuel Oil Coke
Coker
108% Total Yield
Complex refineries can run heavier and more sour crudes while achieving the
highest light product yields and volume gain 11
12. FCC and Hydrocracker Reactors
Fluidized Catalytic Cracker
Reactor Hydrocracker Reactors
Main Column Regenerator
12
13. Cokers
Delayed Coker
Superstructure holds the drill and drill stem
Fluid Coker - Benicia
while the coke is forming in the drum
13
14. Conversion Economics
U.S. Gulf Coast Refinery Margins
30
25
20
15
US $/ Bbl
10
5
0
(5)
(10)
Jan-00 Jan-01 Jan-02 Jan-03 Jan-04 Jan-05 Jan-06 Jan-07
Arab Medium Hydroskimming LLS Cracking Maya Coking
Need conversion capacity to capitalize on sour crude discounts
• Hydroskim – Breakeven or moderate margins; High resid yield
− When margins are positive – increase crude runs
− When margins are negative – decrease crude runs
• Cracking – Better margins; Lower resid yield
• Coking – Best margins; Lowest resid yield
− Maximize heavy crudes
14
15. Desulfurization Basics
Objective
Remove sulfur from light products (gasoline or diesel) to meet air quality
requirements for clean burning fuels
Desulfurization Unit
Desulfurized Light Products
HC
H2
High Sulfur HC-S
HC-S
HC-S
Light H2
Elemental
H2
Products Catalyst
Sulfur Plant Sulfur
(HC-S) • Agricultural
HC-S
HC-S H2S S
S S • Pharmaceutical
H2 S
HC-S
S S
2
H
Hydrogen Unit
LEGEND
H2 LEGEND
H2 H2 HC : : Hydrocarbon
HC Hydrocarbon
H2 1000 or less PSI; H2 : : Hydrogen
H2
H2 H2 Hydrogen
700 F or less
S : : Sulfur
S Sulfur
15
16. Hydrocracking Basics
Objective
Value added upgrading of high sulfur distillates to low sulfur gasoline and ultra
low sulfur jet/diesel to meet air quality requirements for clean burning fuels
Hydrocracking Unit Desulfurized Hydrocrackate Gasoline
HC
H2
High Sulfur HC-S
HC-S
HC-S H2
Distillate H2 Desulfurized Ultra Low Sulfur Jet/Diesel
HC
H2
H2
(HC-S) Catalysts H2 Elemental
H2
Sulfur Plant Sulfur
HC-S H2 H2 HC-S
• Agricultural
H2S S
H2 S S • Pharmaceutical
HC-S S
S S
2
H
Hydrogen Unit
LEGEND
H2 LEGEND
H2 H2 HC : : Hydrocarbon
HC Hydrocarbon
1300+ PSI;
H2 H2 : : Hydrogen
H2
H2 H2 Hydrogen
725 to 780 F
S : : Sulfur
S Sulfur
16
18. Valero Texas City Refinery
Acquired by Valero in 1997 via
purchase of Basis Petroleum from
Solomon, Inc.
Located along Houston’s Deep Water
Ship Channel at the Port of Texas City
Began operations in 1908. Supported
World Wars I and II
Throughput capacity of 245,000
barrels per day of crude and other
feedstocks
Produces gasoline, jet fuel, diesel,
LPG, sulfur and chemical feedstocks
18
19. Valero Texas City Refinery
Staffed by over 500 full-time
employees and 300 continuing
service contractors
Recognized as an “OSHA VPP Star
Site”
Received VPP “Star Among Stars
Status in 2003
Received VPP “Spirit Award” in
2004
19
21. Texas City Capital Investments
Over $900 MM invested in capital improvements and $300 MM for turnaround maintenance at
Texas City since Valero’s acquisition
• Delayed Coker Unit – 45 MBPD Capacity
− Started up in 2003
• Gasoline Desulfurization Unit – 48 MBPD Capacity
− Started up in 2003
• LPG Recovery Unit – 35 MM SCF/D Capacity
− Started up in 2004
• Steam Boilers (3)
− Started up in 2005 and 2006
• Electrical Substation
− Operational in 2006
• Administrative Office and Central Control Center
− Occupied May 2005
• Major plant turnaround just completed ($80 MM Turnaround Maintenance and $70 MM Capital
Improvements).
21
24. Major Refining Processes – Crude
Processing
Definition
• Separating crude oil into different hydrocarbon groups
• The most common means is through distillation
Process
• Desalting – Prior to distillation, crude oil is often desalted to remove
corrosive salts as well as metals and other suspended solids.
• Atmospheric Distillation – Used to separate the desalted crude into specific
hydrocarbon groups (straight run gasoline, naphtha, light gas oil, etc.) or
fractions.
• Vacuum Distillation – Heavy crude residue (“bottoms”) from the atmospheric
column is further separated using a lower–pressure distillation process.
Means to lower the boiling points of the fractions and permit separation at
lower temperatures, without decomposition and excessive coke formation.
24
25. Major Refining Processes – Cracking
Definition
• “Cracking” or breaking down large, heavy hydrocarbon molecules into
smaller hydrocarbon molecules thru application of heat (thermal) or through
the use of catalysts
Process
• Coking – Thermal non–catalytic cracking process that converts low value oils to
higher value gasoline, gas oils and marketable coke. Residual fuel oil from vacuum
distillation column is typical feedstock.
• Visbreaking – Thermal non–catalytic process used to convert large hydrocarbon
molecules in heavy feedstocks to lighter products such as fuel gas, gasoline, naphtha
and gas oil. Produces sufficient middle distillates to reduce the viscosity of the heavy
feed.
• Catalytic Cracking – A central process in refining where heavy gas oil range feeds are
subjected to heat in the presence of catalyst and large molecules crack into smaller
molecules in the gasoline and surrounding ranges.
• Catalytic Hydrocracking – Like cracking, used to produce blending stocks for gasoline
and other fuels from heavy feedstocks. Introduction of hydrogen in addition to a
catalyst allows the cracking reaction to proceed at lower temperatures than in
catalytic cracking, although pressures are much higher.
25
26. Major Refining Processes –
Combination
Definition
• Linking two or more hydrocarbon molecules together to form a large
molecule (e.g. converting gases to liquids) or rearranging to improve the
quality of the molecule
Process
• Alkylation – Important process to upgrade light olefins to high–value
gasoline components. Used to combine small molecules into large
molecules to produce a higher octane product for blending with gasoline.
• Catalytic Reforming – The process whereby naphthas are changed
chemically to increase their octane numbers. Octane numbers are
measures of whether a gasoline will knock in an engine. The higher the
octane number, the more resistance to pre or self–ignition.
• Polymerization – Process that combines smaller molecules to produce high
octane blending stock.
• Isomerization – Process used to produce compounds with high octane for
blending into the gasoline pool. Also used to produce isobutene, an
important feedstock for alkylation.
26
27. Major Refining Processes – Treating
Definition
• Processing of petroleum products to remove some of the sulfur, nitrogen,
heavy metals, and other impurities
Process
• Catalytic Hydrotreating, Hydroprocessing, sulfur/metals removal – Used to
remove impurities (e.g. sulfur, nitrogen, oxygen and halides) from petroleum
fractions. Hydrotreating further “upgrades” heavy feeds by converting
olefins and diolefins to parafins, which reduces gum formation in fuels.
Hydroprocessing also cracks heavier products to lighter, more saleable
products.
27
28. List of Refining Acronyms
AGO – Atmospheric Gas Oil kVA – Kilovolt Amp
ATB – Atmospheric Tower Bottoms LCO – Light Cycle Oil
B–B – Butane–Butylene Fraction LGO – Light Gas Oil
BBLS – Barrels LPG – Liquefied Petroleum Gas
BPD – Barrels Per Day LSD – Low Sulfur Diesel
BTX – Benzene, Toluene, Xylene LSR – Light Straight Run (Gasoline)
CARB – California Air Resource Board MON – Motor Octane Number
CCR – Continuous Catalytic Regenerator MTBE – Methyl Tertiary–Butyl Ether
DAO – De–Asphalted Oil MW – Megawatt
DCS – Distributed Control Systems NGL – Natural Gas Liquids
DHT – Diesel Hydrotreater NOX – Nitrogen Oxides
DSU – Desulfurization Unit P–P – Propane–Propylene
EPA – Environmental Protection Agency PSI – Pounds per Square Inch
ESP – Electrostatic Precipitator RBOB – Reformulated Blendstock for Oxygen Blending
FCC – Fluid Catalytic Cracker RDS – Resid Desulfurization
GDU – Gasoline Desulfurization Unit RFG – Reformulated Gasoline
GHT – Gasoline Hydrotreater RON – Research Octane Number
GOHT – Gas Oil Hydrotreater RVP – Reid Vapor Pressure
GPM – Gallon Per Minute SMR – Steam Methane Reformer (Hydrogen Plant)
HAGO – Heavy Atmospheric Gas Oil SOX – Sulfur Oxides
HCU – Hydrocracker Unit SRU – Sulfur Recovery Unit
HDS – Hydrodesulfurization TAME – Tertiary Amyl Methyl Ether
HDT – Hydrotreating TAN – Total Acid Number
HGO – Heavy Gas Oil ULSD – Ultra–low Sulfur Diesel
HOC – Heavy Oil Cracker (FCC) VGO – Vacuum Gas Oil
H2 – Hydrogen VOC – Volatile Organic Compound
H2S – Hydrogen Sulfide VPP – Voluntary Protection Program
HF – Hydroflouric (adic) VTB – Vacuum Tower Bottoms
HVGO – Heavy Vacuum Gas Oil WTI – West Texas Intermediate
kV – Kilovolt WWTP – Waste Water Treatment Plant
28
29. Safe Harbor Statement
Statements contained in this presentation that state the
Company's or management's expectations or predictions
of the future are forward–looking statements intended to
be covered by the safe harbor provisions of the Securities
Act of 1933 and the Securities Exchange Act of 1934. The
words quot;believe,quot; quot;expect,quot; quot;should,quot; quot;estimates,quot; and
other similar expressions identify forward–looking
statements. It is important to note that actual results could
differ materially from those projected in such forward–
looking statements. For more information concerning
factors that could cause actual results to differ from those
expressed or forecasted, see Valero’s annual reports on
Form 10-K and quarterly reports on Form 10-Q, filed with
the Securities and Exchange Commission, and available
on Valero’s website at www.valero.com.
29