Slides for the eLearning course Separation and purification processes in biorefineries (https://open-learn.xamk.fi) in IMPRESS project (https://www.spire2030.eu/impress).
Section: Distillation
Subject: 0.2 Introduction to distillation.
The presentation details the process of combustion in a 500 MW Coal based Thermal Power Plant where the main fuel is Pulverised coal. It details about the combustion of coal partical in the furnace and also the combustion equations related to the process, the excess air that is supplied.
Slides for the eLearning course Separation and purification processes in biorefineries (https://open-learn.xamk.fi) in IMPRESS project (https://www.spire2030.eu/impress).
Section: Distillation
Subject: 2.1 Material balances
Slides for the eLearning course Separation and purification processes in biorefineries (https://open-learn.xamk.fi) in IMPRESS project (https://www.spire2030.eu/impress).
Section: Distillation
Subject: 0.2 Introduction to distillation.
The presentation details the process of combustion in a 500 MW Coal based Thermal Power Plant where the main fuel is Pulverised coal. It details about the combustion of coal partical in the furnace and also the combustion equations related to the process, the excess air that is supplied.
Slides for the eLearning course Separation and purification processes in biorefineries (https://open-learn.xamk.fi) in IMPRESS project (https://www.spire2030.eu/impress).
Section: Distillation
Subject: 2.1 Material balances
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
Episode 3 : Production of Synthesis Gas by Steam Methane ReformingSAJJAD KHUDHUR ABBAS
Episode 3 : Production of Synthesis Gas by Steam Methane Reforming
History of Synthesis Gas
In 1780, Felice Fontana discovered that combustible gas develops if water vapor is passed over carbon at temperatures over 500 °C. This CO and H2 containing gas was called water gas and mainly used for lighting purposes in the19th century.
As of the beginning of the 20th century, H2/CO-mixtures were used for syntheses of hydrocarbons and then, as a consequence, also called synthesis gas.
Haber and Bosch discovered the synthesis of ammonia from H2 and N2 in 1910 and the first industrial ammonia synthesis plant was commissioned in 1913.
The production of liquid hydrocarbons and oxygenates from syngas conversion over iron catalysts was discovered in 1923 by Fischer and Tropsch.
Much of the syngas conversion processes were being developed in Germany during the first and second world wars at a time when natural resources were becoming scare and alternative routes for hydrogen production, ammonia synthesis, and transportation fuels were a necessity.
In 1943/44, this was applied for large-scale production of artificial fuels from synthesis gas in Germany.
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
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
Episode 3 : Production of Synthesis Gas by Steam Methane ReformingSAJJAD KHUDHUR ABBAS
Episode 3 : Production of Synthesis Gas by Steam Methane Reforming
History of Synthesis Gas
In 1780, Felice Fontana discovered that combustible gas develops if water vapor is passed over carbon at temperatures over 500 °C. This CO and H2 containing gas was called water gas and mainly used for lighting purposes in the19th century.
As of the beginning of the 20th century, H2/CO-mixtures were used for syntheses of hydrocarbons and then, as a consequence, also called synthesis gas.
Haber and Bosch discovered the synthesis of ammonia from H2 and N2 in 1910 and the first industrial ammonia synthesis plant was commissioned in 1913.
The production of liquid hydrocarbons and oxygenates from syngas conversion over iron catalysts was discovered in 1923 by Fischer and Tropsch.
Much of the syngas conversion processes were being developed in Germany during the first and second world wars at a time when natural resources were becoming scare and alternative routes for hydrogen production, ammonia synthesis, and transportation fuels were a necessity.
In 1943/44, this was applied for large-scale production of artificial fuels from synthesis gas in Germany.
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
4. A gaseous fuel contains the following by mole 31.3 C2H6; 67.6 .pdfpasqualealvarez467
4. A gaseous fuel contains the following by mole: 31.3% C2H6; 67.6% CH4; 1.1% N2.
Determine
i. the gravitational stoichiometric air.
ii. The DRY molar composition of the combustion products if the fuel is burned with 150%
theoretical air. Assume complete combustion of the fuel
iii. The WET analysis of the products by mass if the fuel is burned with 15% less air.
Solution
2C2H6 + 7O2 = 2CO2 + 3H2O------ eqn i
0.313 moles of C2H6 + 1.0955 moles of O2 = 0626 moles of CO2 +0.939 moles of H20(here %
of moles is taken as fractions )
given 31.3% of ethane in fuel so moles of O2 = 7/2 *(0.313)= 1.0955
moles of CO2 = 2*0.313 = 0.626
moles of H2O = 3*0.313 = 0.939
CH4+ 2 O2 = CO2 + H2O ------- eqn ii
0.676 moles of methane + 1.352 moles of oxygen = 0.676 moles of CO2 + 0.676 moles of H2O
moles of O2 = 0.676*2 = 1.352
assume air composition
oxygen = 21% = 0.21
nitrogen = 79% = 0.79
moleculae weight of air = 29 g
Total moles of oxygen required for reaction = 1.0955 + 1.352 = 2.4474
= 2.4475 * 16 = 39.16 g ( 1 mole O2 = 16g )
quantity of air needed = 39.16/0.21 = 186.476 g ( in air 21% of O2 is present )
no of moles of air required to burn the enitre fuel = 186.476 / 29 = 6.4137 . ( Gravitational
stoichiometric air )
at dry condition 150% of air is supplied so net moles of air = 6.4137*1.5 = 9.6206
therefore
total moles of CO2 = 0.626+0.676 =1.302 from eqn i & ii
no of moles of nitrogen in 9.6206 moles of air = (9.6206*29 *0.79)/14 =15.74 (molecular weight
of nitrogen = 14 g)
total moles of N2 = 0.011+15.7434 = 15.7534
total quanitity of O2 = (9.6206-6.4137)*29*0.21 =19.53
no of moles of oxygen = 19.53/16 = 1.2206
so Dry molar composition of the combustion products is
%moles of CO2 = 1.302 / ( 1.302+15.7534+1.2206) = 1.302 / 18.276 = 0.0712
%moles of N2 = 15.7534 / ( 1.302+15.7534+1.2206) = 15.7534/18.276 = 0.8619
%moles of O2 = 1.2206/ ( 1.302+15.7534+1.2206) = 1.2206/18.276 =0.06678
At Wet analysis 15% less air is supplied
so total moles of air = 6.4137*0.85 = 5.4516
Wet molar composition of products
moles ofN2 = 0.011
moles of of CO2 = (0.626+0.676)*0.85 = 1.01067 from eqn i &ii
moles of H2O = (0.939+0.676)*0.85 = 1.37275 from eqn i &ii
moles of C2H6 = 0.313*0.15 = 0.04695
moles of CH4 = 0.676*0.15 = 0.1014
molar composition on wet analysis
% moles of N2 = 0.011 / ( 0.011+1.1067+1.37275+0.04695+0.1014) = 0.011/2.6388= 0.0041
% moles of CO2 = 1.1067 / ( 0.011+1.1067+1.37275+0.04695+0.1014) = 1.1067 / 2.6388 =
0.4193
% moles of H2O = 1.37275 / ( 0.011+1.1067+1.37275+0.04695+0.1014) = 1.37275 / 2.6388=
0.52
% moles of C2H6 = 0.04695 / ( 0.011+1.1067+1.37275+0.04695+0.1014) = 0.04695 /
2.6388=0.0177
% moles of CH4 = 0.1014/ ( 0.011+1.1067+1.37275+0.04695+0.1014)= 0.1014/2.6388 = 0.0384.
Combustion is a chemical process in which a substance reacts rapidly with oxygen and gives off heat. The original substance is called the fuel, and the source of oxygen is called the oxidizer. The fuel can be a solid, liquid, or gas, although for airplane propulsion the fuel is usually a liquid. The oxidizer, likewise, could be a solid, liquid, or gas.
About
Indigenized remote control interface card suitable for MAFI system CCR equipment. Compatible for IDM8000 CCR. Backplane mounted serial and TCP/Ethernet communication module for CCR remote access. IDM 8000 CCR remote control on serial and TCP protocol.
• Remote control: Parallel or serial interface.
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• Compatible with commercial and Defence aviation CCR system.
• Remote control system for accessing CCR and allied system over serial or TCP.
• Indigenized local Support/presence in India.
• Easy in configuration using DIP switches.
Technical Specifications
Indigenized remote control interface card suitable for MAFI system CCR equipment. Compatible for IDM8000 CCR. Backplane mounted serial and TCP/Ethernet communication module for CCR remote access. IDM 8000 CCR remote control on serial and TCP protocol.
Key Features
Indigenized remote control interface card suitable for MAFI system CCR equipment. Compatible for IDM8000 CCR. Backplane mounted serial and TCP/Ethernet communication module for CCR remote access. IDM 8000 CCR remote control on serial and TCP protocol.
• Remote control: Parallel or serial interface
• Compatible with MAFI CCR system
• Copatiable with IDM8000 CCR
• Compatible with Backplane mount serial communication.
• Compatible with commercial and Defence aviation CCR system.
• Remote control system for accessing CCR and allied system over serial or TCP.
• Indigenized local Support/presence in India.
Application
• Remote control: Parallel or serial interface.
• Compatible with MAFI CCR system.
• Compatible with IDM8000 CCR.
• Compatible with Backplane mount serial communication.
• Compatible with commercial and Defence aviation CCR system.
• Remote control system for accessing CCR and allied system over serial or TCP.
• Indigenized local Support/presence in India.
• Easy in configuration using DIP switches.
Vaccine management system project report documentation..pdfKamal Acharya
The Division of Vaccine and Immunization is facing increasing difficulty monitoring vaccines and other commodities distribution once they have been distributed from the national stores. With the introduction of new vaccines, more challenges have been anticipated with this additions posing serious threat to the already over strained vaccine supply chain system in Kenya.
Cosmetic shop management system project report.pdfKamal Acharya
Buying new cosmetic products is difficult. It can even be scary for those who have sensitive skin and are prone to skin trouble. The information needed to alleviate this problem is on the back of each product, but it's thought to interpret those ingredient lists unless you have a background in chemistry.
Instead of buying and hoping for the best, we can use data science to help us predict which products may be good fits for us. It includes various function programs to do the above mentioned tasks.
Data file handling has been effectively used in the program.
The automated cosmetic shop management system should deal with the automation of general workflow and administration process of the shop. The main processes of the system focus on customer's request where the system is able to search the most appropriate products and deliver it to the customers. It should help the employees to quickly identify the list of cosmetic product that have reached the minimum quantity and also keep a track of expired date for each cosmetic product. It should help the employees to find the rack number in which the product is placed.It is also Faster and more efficient way.
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.
CFD Simulation of By-pass Flow in a HRSG module by R&R Consult.pptxR&R Consult
CFD analysis is incredibly effective at solving mysteries and improving the performance of complex systems!
Here's a great example: At a large natural gas-fired power plant, where they use waste heat to generate steam and energy, they were puzzled that their boiler wasn't producing as much steam as expected.
R&R and Tetra Engineering Group Inc. were asked to solve the issue with reduced steam production.
An inspection had shown that a significant amount of hot flue gas was bypassing the boiler tubes, where the heat was supposed to be transferred.
R&R Consult conducted a CFD analysis, which revealed that 6.3% of the flue gas was bypassing the boiler tubes without transferring heat. The analysis also showed that the flue gas was instead being directed along the sides of the boiler and between the modules that were supposed to capture the heat. This was the cause of the reduced performance.
Based on our results, Tetra Engineering installed covering plates to reduce the bypass flow. This improved the boiler's performance and increased electricity production.
It is always satisfying when we can help solve complex challenges like this. Do your systems also need a check-up or optimization? Give us a call!
Work done in cooperation with James Malloy and David Moelling from Tetra Engineering.
More examples of our work https://www.r-r-consult.dk/en/cases-en/
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
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.
Overview of the fundamental roles in Hydropower generation and the components involved in wider Electrical Engineering.
This paper presents the design and construction of hydroelectric dams from the hydrologist’s survey of the valley before construction, all aspects and involved disciplines, fluid dynamics, structural engineering, generation and mains frequency regulation to the very transmission of power through the network in the United Kingdom.
Author: Robbie Edward Sayers
Collaborators and co editors: Charlie Sims and Connor Healey.
(C) 2024 Robbie E. Sayers
Forklift Classes Overview by Intella PartsIntella Parts
Discover the different forklift classes and their specific applications. Learn how to choose the right forklift for your needs to ensure safety, efficiency, and compliance in your operations.
For more technical information, visit our website https://intellaparts.com
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Event Management System Vb Net Project Report.pdfKamal Acharya
In present era, the scopes of information technology growing with a very fast .We do not see any are untouched from this industry. The scope of information technology has become wider includes: Business and industry. Household Business, Communication, Education, Entertainment, Science, Medicine, Engineering, Distance Learning, Weather Forecasting. Carrier Searching and so on.
My project named “Event Management System” is software that store and maintained all events coordinated in college. It also helpful to print related reports. My project will help to record the events coordinated by faculties with their Name, Event subject, date & details in an efficient & effective ways.
In my system we have to make a system by which a user can record all events coordinated by a particular faculty. In our proposed system some more featured are added which differs it from the existing system such as security.
2. P-1
The flue gas from an industrial furnace has the following
composition by volume
CO2: 11.73%, CO: 0.2 %, SO2: 0.09%, O2: 6.81% and
N2: 81.17 %
Calculate the percentage excess air employed in the
combustion if the loss of carbon in the clinker ash is 1%
of the fuel used and the fuel has the following
composition by weight:
C: 74%, H2: 5 %, O2: 5%, N2: 1%, S: 1%, H2O: 9%, ash
: 5%
•
•
•
•
3. P-1
Basis: 100 kg of the fuel
C + O2 => CO2
H2 +1/2 O2 => H2O
S + O2 => SO2
Oxygen Balance:
•
•
•
•
•
• Oxygen required for complete combustion
=74/12 + 5/2 X 1/2 + 1/32=7.447 kg mole
Oxygen present in fuel=5/32=0.157 kg mole
Net oxygen from air= 7.447-0.157=7.29 kg mole
4. P-1
• Carbon balance
Carbon lost in clinker and ash = 1 kg
Carbon burnt= 74-1= 73 kg = 73/12=6.08 kg
Assume z kg moles of flue gas are formed
By carbon balance (0.1173+0.002)*Z=6.08
z=50.96 kg moles
atom
So
N2
N2
N2 in flue gas= 50.96 *0.8117=41.36
from fuel= 1 kg=0.036 kg moles
from air = 41.36-0.036=41.324
Oxygen from air =41.324 * 21/79=10.98 kg
Excess oxygen = 10.98-7.29= 3.69
mole
5. P-1
Excess oxygen = 10.98-7.29= 3.69 kg mole
Percentage excess air used = percentage excess oxygen
used
= excess/theoretical* 100= 3.69/7.29* 100= 50.62
6. P-2
is burnt with 10 % excess
•
•
•
•
•
•
Octane air. Calculate
Air to fuel
Air to fuel
Weight of
ratio by weight
ratio by volume
dry exhaust gas formed per unit weight of fuel
Moles of oxygen in the exhaust gas per unit weight of fuel
Moles of water vapour in exhaust gas per unit weight of
fuel
Volume of exhaust gas at 1 atmosphere and 260 C per
unit weight of fuel
•
The specific gravity of octane may be taken as 0.7
7. P-3
A producer gas with the composition by volume CO: 27.3 %, CO2:5.4%,
O2: 0.6 %, N2 : 66.7% is burnt with 20 % excess air. If the combustion
•
is 98% complete, calculate the composition by volume of
Solution:
Basis: 100 kg mole of producer gas burnt
the flue gases
•
•
Oxygen balance:
O2 required for CO combustion= 27.3*0.5=13.65 kg mole
O2 present in fuel = 0.6 kg mole
Net O2 required = 13.65 – 0.6 = 13.05 kg mole
O2
O2
O2
supplied by 20 % excess air = 13.05*1.20= 15.66 kg mole
used for 98% combustion of CO=13.05*0.98=12.8 kg mole
excess = 15.66 -12.8 =2.86 kg mole
8. P-3
Nitrogen balance:
N2 from air = 15.66 * 79/21= 58.91 kg mole
N2 from producer gas = 66.7 kg mole
Total N2 in flue gas = 66.70 + 58.91=125.61 kg mole
CO2
CO2
CO2
balance:
from producer gas 5.4 kg mole
from combustion of CO = 27.3 *0.98= 26.75 kg mole
Total CO2 in flue gas = 5.4 + 26.75 = 32.15 kg mole
CO
CO
CO
balance:
burnt = 26.75 kg mole
left = 27.3 – 26.75 = 0.55 kg mole
10. P-4
A furnace is fired with a natural gas that consists
entirely of hydrocarbons( no inert or sulphur). The
analysis of the flue gas is 9.5 % CO2, 2.0% O2
and 1.8% CO
What is the molar ratio of net hydrogen to carbon
in the fuel?
What percentage of excess air is being used?
•
•
•
11. P-4
• Solution:
Basis: 100 kg of dry flue gas
N2 =100 –(9.5+1.8+2.0) =86.7
Oxygen balance:
O2
O2
O2
supplied by air = 86.7 *21/79 =23.05 kg mole
in dry flue gas= 9.5+1.8/2 +2 =12.4 kg mole
unaccounted ( reacted with H2)= 23.05-12.4
=10.65 kg mole
Moles of H2 reacted = 10.65 * 2 =21.3
Amount of carbon = 9.5 + 1.8 = 11.3 kg atoms
Moles of H2/Moles of C= 21.3/11.3 =1.18
Moles of O2 required for complete combustion=moles
=10.65 + 11.3=21.95
Amount of excess O2 = 23.05 -21.95=1.1 kg mole
% excess air = 1.1/21.95*100 = 5
for H2 +moles for C
12. P-5
The exhaust gas from a hydrocarbon fuel oil fired
furnace show 10.2% CO2, 7.9% O2 and 81.9%
N2. Calculate
%excess air used
Kg of dry air supplied per kg of oil burnt
•
•
•
13. P-6
Determine the flue gas analysis and air/fuel ratio
by weight when a fuel oil with 84.9% carbon,
11.4% hydrogen, 3.2% sulphur, 0.4% oxygen and
0.1% ash by weight is burnt with 20 % excess air.
Assume complete combustion.
•
14. P-7
A boiler is fired using 200 kg/hr of a pure saturated
hydrocarbon gas CnHm at atmospheric pressure and 20
C. The dry analysis of the flue gas which leaves the boiler
at atmospheric pressure and 300 C is CO2: 12%, O2: 3%
•
and N2 :85%. Estimate the formula of the fuel and total
volumetric flow rate of the gas
Solution:
Basis: 100 kg mole of dry flue gas
Oxygen Balance
•
•
•
N2 in flue gas = 85 kg mole
O2 supplied by air = 85 *21/79=22.59 kg mole
15. P-7
•
•
O2 reported in
flue gas = O2 in CO2 + O2 as O2
=12 + 3.0 =15.0 kg mole
O2 unaccounted (reacted with H2) =22.59 – 15.0
= 7.59 kg mole
H2 reacted = 7.59 * 2=15.18 kg mole
= 30.36 kg atoms
Amount of carbon = 12 kg atoms
Amount of hydrogen=30.36 kg atoms
Ratio=Atoms of H/Atoms of C=30.36/12=2.53
Paraffin formula=CnH2n+2
(2n+2)/n=2.53
So n =3.77 ~ 4
Hence the fuel is C4H10
Volumetric flow rate =?
Amount of fuel = 200/58 3.45 kg mole
Assuming ideal gas law, volume at 20 C and 1 atmosphere is :
V=nRT/P=3.45*0.08206*293/1 = 82.95 m3/hr
16. P-8
A furnace is fired with a fuel having the volumetric
composition H2: 52%, CH4: 30 %, CO: 8%, C3H6: 3.6%,
•
CO2: 2%, O2: 0.4% and rest N2.
• Using a certain quantity of air in excess over stoichiometric.
Complete combustion of the gas is achieved giving a dry
waste gas of 5 m3 per m3 of fuel burned. Estimate
Composition by volume of dry waste gas formed
Per cent excess air used
Weight of water formed per m3 of gas burned
•
•
•
17. P-8
Solution:
Basis: 100 kg mole of fuel gas
CH4 + 2 O2 => CO2 + 2H2O
CO + 1/2O2 => CO2
C3H6 + 4.5 O2 => 3 CO2 + 3H2O
H2 + ½ O2 => H2O
Oxygen balance
O2
O2
O2
O2
required
required
required
required
for
for
for
for
CO=8*1/2=4 kg mole
CH4=30*2=60 kg mole
C3H6=3.6*4.5=16.2 kg mole
H2 = 52*1/2=26 kg mole
Total O2 required =106.2 kg mole
O2 in fuel =0.4 kg mole
18. P-8
Net O2 required from air =106.2 -0.4 =105.8 kg mole
DRY Flue Gas formed with theoretical air:
CO2 formed=8.0(from CO) + 30.0 (from CH4) + 10.8
C3H6) +2.0(present in fuel)
=50.8 kg mole
N2 from air = 105.8 * 79/21= 398 kg mole
Total N2 = 398 + 4 (present in fuel) = 402 kg mole
(from
Total amount of dry flue gas (with theoretical air) =402+50.8
=452.8 kg mole
Flue gas actually produced=5 m3/m3 of fuel
Total dry flue gas produced=100*5 =500 kg mole
Excess air=500 – 452.8 =47.2 kg mole
Theoretical air =105.8 *100/21=503.81 kg mole
19. P-8
Theoretical air =105.8 *100/21=503.81 kg mole
a)
b)
Air
N2
% excess air = 47.2/503.8*100=9.39
Composition of flue gas:
used = 503.81 + 47.2 = 551.01 kg mole
from air = 551.01 *79/100 = 435.29 kg mole
Total N2 = 435.29 + 4.0 =439.29 kg mole
Excess O2 = 47.2 *21/100 =9.91 kg mole
Flue gas analysis: constituent Amount kg
mole
Vol%
CO2
O2
N2
50.8
9.91
439.29
10.16
1.98
87.86
total 500 100
20. P-8
(C) Amount of water formed = 52.0 (from H2) + 60 (from
CH4) + 10.8 ( from C3H6) = 122.8 kg mole = 122.8 *18
=2210.4 kg
Amount of gas burned=100 kg mole=22.4*100 m3 at NTP
Weight of water formed/m3 gas burned=2210.4 kg /2240 m3
=0.987 kg of water/m3 of gas
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•
•
21. P-9
The dry flue gas from an oil fired furnace has the
composition of 11.2 % CO2, 5.8% O2, 83% N2. Calculate
% excess air
•
•
•
•
Weight of combustion air
Assume fuel has 82% C,
impurities.
Solution:
Basis: 100 kg of oil fired
Oxygen balance:
per kg of oil fired
12 % H2, 3 % S and balance is
•
•
•
•
•
•
•
O2
O2
O2
required
required
required
for
for
for
82 kg of carbon=82/12=6.833 kg mole
12 kg of H2 =12/2*0.5=3 kg mole
3 kg of S =0.094 kg mole
total O2 required = 6.833 + 3.0 + 0.094 =9.927 kg mole
22. P-9
Let z kg mole of dry flue gas is formed
•
•
•
•
•
•
•
•
•
•
•
Carbon balance: 0.112* z (out) =6.833 (in)
So z =61.0 kg mole
Amount of N2 in flue gas = 61 * 0.83 = 50.83 kg mole
O2 from air = 50.83 *21/79 =13.46 kg mole
O2 excess = 13.46 – 9.927 =3.533 kg mole
% excess air =% excess O2 = 3.533/9.927*100=35.6%
Amount of combustion air = 50.63*100/79=64.09 kg mole
Molecular weight of air =28.84
Amount of air in kg =64.09*28.84=1848.36 kg
Mass of air in kg/mass of fuel in kg=1848.36/100=18.48
23. P-10
A fuel gas containing 97% methane and 3% N2 by volume
•
is burned in boiler furnace with 200% excess air, 85% of
methane goes to CO2, 10% to CO and
unburnt.
Calculate the composition of stack gas
5% remains
•
Solution:
Basis: 100 kg mole of fuel gas
CH4 + 2 O2 => CO2 + 2H2O ….. (1)
2 CH4 + 3 O2 => 2 CO + 4 H2O …..(2)
O2 required for complete combustion= 97*2=194 kg mole
O2 supplied by 200 % excess air = 3*194 = 582 kg mole
Reaction (1) is 85% complete and (2) is 10% complete
24. P-10
Methane converted by reaction (1) = 97 *0.85=82.45 kg mole
Methane converted by reaction (2) = 97*0.1=9.7 kg mole
Oxygen used in reaction (1) & 2= 82.5*2+9.7*3/2=179.45 kg mole
stack gas:
CO2 formed = 82.45 kg mole
CO formed = 9.7 kg mole
CH4 unconverted = 5 kg mole
N2 from air = 582 * 79/21=2189.43 kg mole
N2 from fuel = 3.0 kg mole
Total N2 in flue gas =2189.43 + 3.0=2192.43 kg mole
H2O formed = 82.25*2(by reaction 1) + 9.7*4/2(by reaction 2)
=184.3 kg mole
Excess oxygen = 582 – 179.45 = 402.55 kg mole
25. P-10
stack gas analysis
constituent kg mole Mole %
CO2 82.45 2.87
CO 9.70 0.34
CH4 5 0.17
O2 402.55 13.99
N2 2192.43 76.22
H2O 184.30 6.41
Total 2676.28 100