Thursday, 24 May 2018

Techanical Handwritten Notes for Mechanical Engineering


Download  Good quality Handwritten Notes for Mechanical Engineering branch which is based on GATE and ESE syllabus. Hope it will help your GATE/ESE preparation!



Sr No
     Subject        
   Download Link   
  
1.

  Aptitude  

2.

  Fluid Mechanics    
   
3.

Heat Transfer
   
4.

 Thermodynamics
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5.

 Power Plant Engineering

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 6.



Refrigeration & Air Conditioning

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7.

I C Engines


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8.

Theory of Machines
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 9.  

Machine Design
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10.

Strength of Materials  
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11.

Material Science
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12.



Operations Research & Industrial Engineering

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13.

Production Engineering
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14.

Renewable Sources of Energy
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16.

Mechatronics and Robotics
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17.

Engineering Mathematics
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Sunday, 20 May 2018

Radiation-II


THE VIEW FACTOR/SHAPE FACTOR


It is a purely geometric quantity and is independent of the surface properties and temperature. It is also known as configuration factor and angle factor.

The view factor from a surface i to a surface j is denoted by Fi → j or just $F_{ij}$, and is defined as
$F_{ij}$ = the fraction of the radiation leaving surface i that strikes surface j directly
\[F_{ij} = \frac{Q_{ij}}{Q_i}\]
Here,            $Q_{ij}$ =  fraction of rate of energy leaving surface i reaching surface j
                    Qi = Rate of total energy radiated by surface i

  • In general, 0 ≤ $F_{ij}$ ≤ 1.
  • The view factor from a surface to itself is zero for plane or convex surfaces and nonzero for concave surfaces.


Reciprocity Relation

\[\boxed{A_1F_{12} = A_2F_{21}}\]

Summation Rule

The sum of the view factors from surface i of an enclosure to all surfaces of the enclosure, including to itself, must equal unity.
\[\boxed{\sum^N_{j =1} F_{ij}  =1}\]

$F_{11} = 0$

$F{11} + F_{12} = 1$   (Summation Rule)

hence $F_{12} = 1$

$A_1F{12} = A_2F_{21}$   (Reciprocity Rule)

$F_{21} = \frac{A_1}{A_2}$

$F_{21} + F_{22} = 1$   (Summation Rule)  

$F_{22} = 1 - F_{21} = 1 - \frac{A_1}{A_2}$




Superposition Rule


The view factor from a surface i to a surface j is equal to the sum of the view factors from surface i to the parts of surface j. 

Note : The reverse of this is not true.

 \[F_{1(23)} = F_{12} + F_{13}\]






Symmetry Rule


This Rule can be expressed as two (or more) surfaces that possess symmetry about a third surface will have identical view factors from that surface.






The Crossed-Strings Method



View Factors between Infinitely Long Surfaces is given by
\[F_{12} = \frac{(L_5 +L_6) -(L_3 + L_4)}{2*L_1}\]

\[F_{ij} = \frac{\sum (Crossed \quad Strings) - \sum (Uncrossed \quad Strings)}{2*(String \quad on \quad surface 'i')}\]






Net Radiation Heat Transfer to or from a Surface


Net Energy Leaving a Surface

The net energy leaving from the surface will be equal to the difference between the energy leaving a surface and the energy received by a surface 
\[Q_i = A_i(J_i -G_i)\]
\[J = ε E_b + ρG\]
If Surface is opaque, ρ = 1 – α 

J = ε Eb + (1 – α) G



we get,   $Q_i = \frac{E_b - J_i}{R_i}$ and $R_i = \frac{1-ε_i}{A_iε_i}$ is the surface resistance to the radiation.

Net Exchange Between Surfaces


The net rate of radiation heat transfer from surface i to surface j can be expressed as
\[Q_{ij} = A_iJ_iF_{ij} - A_jJ_jF_{ji}\]
\[Q_{ij} = \frac{J_i - J_j}{R_{ij}}\]
where $R_{ij}= \frac{1}{A_iF_{ij}}$ is the space resistance to the radiation.

Electrical circuit representation of two surfaces which can see each other nothing else


Total resistance      $R_t = \frac{1-ε_1}{ε_1A_1} + \frac{1}{A_1F_{12}} + \frac{1-ε_2}{ε_2A_2}$
\[Q_{12} = \frac{E_{b1} - E_{b2}}{R_t}\]

Radiation Shields

Assume two flat infinite long flate surfaces 1 and 2 have N shields in between.


Net Heat Transfer without any shield:
\[Q = \frac{A \sigma (T_1^4 - T_2^4)}{\frac{1}{ε_1} + \frac{1}{ε_2} -1}\]

Net Heat transfer with N shields
\[Q = \frac{A \sigma (T_1^4 - T_2^4)}{(\frac{1}{ε_1} + \frac{1}{ε_2} -1) + \sum^N_{j=1}(\frac{1}{ε_{j,1}} + \frac{1}{ε_{j,2}} -1) }\]


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If you have any query, ask in comments.

Saturday, 19 May 2018

Radiation


Radiation is the mode of heat transfer across a system boundary due to a temperature difference in the form of electromagnetic waves as a result of change in the electronic configurations of the atoms and molecules. Radiative heat transfer does not require a medium to pass through; thus, it is the only form of heat transfer present in vacuum.

Electromagnetic Spectrum


All types of electromagnetic waves are classified in terms of wavelength and are propagated at the speed of light (c = 3 x 10^8 m/s).

Electromagnetic Spectrum


Stefan-Boltzman Law


The emissive power of a black body is proportional to absolute temperature to the fourth power.
\[ \boxed{E_b = σ T^4}\]
where:          Eb = Emissive Power, the gross energy emitted from an ideal surface per unit area, time 
  σ = Stefan Boltzman constant, $5.67X10^{-8} W/m^2 K^4$
T = Absolute temperature of the emitting surface, K.

Plank’s Law

\[E_{bλ} = \frac{C_1}{λ^5(e^{\frac{C_2}{λT}}-1)}\]
$C_1 = 2 \pi h c^2 = 3.742 × 10^8 Wμm^4 / m2 $
$C_2 = h c/k = 1.439 × 10^4 μm-K $

$E_{bλ}$ = Monochromatic (single wavelength)  Emissive Power of a black body
c = speed of light = 3x 10^8 m/s
h = Plank's constant = 6.625 x 10^-34 J-s
λ = Wavelength, μm
k = Boltzmann constant = 1.3805 x 10^-23 J/K
T = Absolute temperature, K

An implicit definition Monochromatic (single wavelength) Emissive Power, $E_{bλ}$  is given by
\[E_b = \int^∞_0 E_{bλ}. dλ\]  


  • We can obtain Stefan-Boltzmann Law by integrating Plank's law over all wavelengths.

Wien Displacement Law



It state that the product of the temperature(T) of a black body and the wavelength(λm) at which the maximum value of monochromatic emissive power occurs, is constant.

\[λ_m T = Constant = 2897  μm.K\]




















Some Definitions


Black Body

A black body is defined as a perfect emitter and absorber of radiation. It absorbs all incident radiation regardless of wavelength and direction.

Diffuse Surface

A surface is said to be diffuse if its properties are independent of direction.

Gray Surface

A surface is said to be gray if its properties are independent of wavelength.

Radiation Intensity (I)

It is defined as the energy emitted from an ideal body, per unit projected area on a plane normal to the direction of radiation, per unit time, per unit solid angle. 
\[I = \frac{dq}{dA cos θ d \Omega}\]

Emissivity (ε)

Real surfaces have emissive power, E somewhat less than that of ideal surface (black body). It is defined as the ratio of Emissive power of any body to the Emissive power of a black body of equal temperature.
\[ε = \frac{E}{E_b}\]
Note:
  • For a black body ε = 1, for white body ε = 0.
  • Value of ε varies from 0 to 1.
  • Emissivity may vary with temperature and wavelength.

Receiving Properties


Irradiation(G)

Total incident radiation on a surface from all directions per unit time and per unit area of surface.

  1. The fraction of irradiation absorbed by the surface is called the absorptivity(α),
  2. the fraction reflected by the surface is called the reflectivity (ρ), and
  3. the fraction transmitted is called the transmissivity (τ). For opaque body τ =0.
\[G_{abs} + G_{ref} + G_{tr} = G\]
\[\boxed{α + ρ + τ = 1}\]

Radiosity (J)

It is defined as the radiation energy leaving from a surface per unit time, per unit area of surface. 
\[J = E +  ρG\]

Note:  For a black body J = Eb, since it absorbs all incident radiation and hence no reflection.

Kirchhoff's Law

The emissivity of a body is equal to its absorptivity whenever body is in thermal equilibrium with its surroundings. We can say a good absorber is a good emitter.
\[\boxed{ α = ε}\]

Intensity of Radiation and Lambert's Cosine Law

According to Lambert's Cosine Law, the radiant intensity observed from an ideal ideal diffuse surface is directly proportional to the cosine of the angle of emission (θ).
\[I = I_n cos(θ)\]

  • Emissive power of a black body is $\pi$ times the intensity of radiation.
\[E_b = \pi I_b\]


Monday, 14 May 2018

General Studies and Engineering Aptitude - Hand Written Notes



Download Hand Written Notes For General Studies and Engineering Aptitude (IES Stage I - Paper I, All Branches)

1. Engineering Aptitude

2.Engineering Mathematics and Numerical Analysis

3. General Principles of Design, Drawing, Importance of Safety

4. Standards and Quality practices

5. Basics of Energy and Environment

6. Basics of Project Management

7. Basics of Material Science and Engineering

8. Information and Communication Technologies (ICT)

9. Ethics and values in Engineering profession



MOHIT CHOUKSEY NOTES:


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Boiling and Condensation

Boiling


  • Boiling is a liquid to vapor change process just like evaporation.
  • Evaporation occurs at the liquid–vapor interface when the vapor pressure is less than the saturation pressure of the liquid at a given temperature. Boiling occurs at the solid–liquid interface when a liquid is brought into contact with a surface maintained at a temperature sufficiently above the saturation temperature of the liquid.
  • Evaporation involves no bubble formation or bubble motion.

Boiling and Evaporation Example

Classification of Boiling

  1. Pool Boiling:  Boiling is called pool boiling when bulk fluid motion is absence. Fluid motion is due to natural convection and bubble-induced mixing.
  2. Flow Boiling: Boiling is the presence of bulk fluid motion is called flow boiling (Forced Convection Boiling). Fluid motion is induced by external means such as pump, as well as by bubble-induced mixing. 
  3. Subcooled Boiling: When the temperature of the liquid is below the saturation temperature.
  4. Saturated Boiling: When the temperature of the liquid is equal to the saturation temperature.

The Boiling Curve


In a typical boiling curve, four different boiling regimes are observed: natural convection boiling, nucleate boiling, transition boiling, and film boiling depending on the excess temperature $ΔT_{excess} = T_s - T_{sat}$.

Boiling Curve of water at 1 atm

Natural Convection Boiling (to Point A)

  • Liquid is slightly superheated in this case (a metastable condition) and evaporates when it rises to the free surface.
  • Liquid motion is due to natural convection.

Nucleate Boiling (between Points A and C)

  • Bubbles start forming at point A and increases number of nucleation sites as we move towards point C.
  • Region A–B –– isolated bubbles are formed and heat flux rise sharply with increasing $ΔT_{excess}$.
  • Region B–C –– Increasing number of nucleation sites causes bubble interactions and coalescence into jets and column. Heat flux increases at  lower rate and maximum at point C.

Transition Boiling(between Points C and D)

  • When $ΔT_{excess}$ increases past point C, heat flux decreases because a large fraction of the heater surface is covered by a vapor film, which acts as an insulation.
  • The transition boiling regime, which is also called the unstable film boiling regime.

Film Boiling (beyond Point D)

  • At point D, where the heat flux reaches a minimum is called the Leidenfrost point.
  • Heat transfer is by conduction and radiation across the vapor blanket, therefore,  heat transfer rate increases with increasing excess temperature.


Burnout Phenomenon


  • A typical boiling process does not follow the boiling curve beyond point C.
  • Any attempt to increase the heat flux beyond point C will cause the operation point on the boiling curve to jump suddenly from point C to point E.
  • Surface temperature that corresponds to point E is beyond the melting point of most heater materials, and burnout occurs.
  • Point C on the boiling curve is also called the burnout point, and the heat flux at this point the burnout heat flux.  






Condensation


Condensation occurs when the temperature of a vapor is reduced below its saturation temperature. 

Film condensation 
  • The condensate wets the surface and forms a liquid film that slide down by gravity.

  • This liquid wall serves as resistance to heat transfer. 
\[Re = \frac{(4δ) ρ_l u_m}{µ_l}\]
hydraulic diameter Dh = 4δ

  • Re<30 ─ Laminar (wave-free),

  • 30<Re<1800 ─ Wavy-laminar, 

  • Re>1800 ─ Turbulent.



Dropwise condensation 

  • The condensate forms droplets on the surface and surface covered by countless drops of varying size.

  • Small droplets grow as a result of continued condensation and slide down when they reach a certain size.

  • There is no film to resist heat transfer.

  • Heat transfer rates in dropwise condensation can be achieved more than 10 times higher than in film condensation.

  • Therefore, dropwise condensation is the preferred mode of condensation.

Dropwise condensation is achieved by-
  • Adding a promoting chemical into the vapor (wax, fatty acid),
  • Treating the surface with a promoter chemical,
  • Coating the surface with a polymer such as teflon or a noble metal such as Au, Ag, Rh, Pd, Pt

***
if you have any queries, ask in comments. Do share with other students!

References:

Heat transfer: a practical approach- Cengel Y.A.
Fundamentals of Heat and Mass Transfer -Incropera

Thursday, 10 May 2018

Dimensionless Numbers in Fluid Thermal Engineering


Important dimensionless numbers used in fluid mechanics and heat transfer are given below:-



Dimensionless
Number

 Expression

             Significance



Reynolds Number


$Re =\frac{ρUD}{μ}$ 
  • Re = Inertial force / Viscous force
  • Determines flow is Laminar, Turbulent, or Transient Flow.



Fourier Number




$Fo = \frac{αt}{L^2}$
  • It is a measure of heat conducted through a body relative to heat stored.
  • Larger the Fo, faster propagation of heat through a body
  • It can also be viewed as current time to the time taken to reach steady state



Biot Number


$Bi = \frac{hL}{K_s} = \frac{L/K_s}{1/h}$

  • Ratio of Conductive resistance with in the body to Convection resistance at the surface of the body
  • Bi ≤ 0.1, Lumped system analysis (assumes a uniform temperature distribution throughout the body) is applicable



Nusselt Number


$Nu = \frac{hL}{K_f} = \frac{h ΔT}{K_fΔT/L} = \frac{q_{conv}}{q_{cond}}$

  • Ratio of convective HT to conductive HT coefficient across the boundary layer 
  • The larger the Nu, the more effective the convection. 
  • Used to calculate heat transfer coefficient h


Prandtl Number



$Pr = \frac{ν}{α}= \frac{µC_p}{K}$
  • Ratio of momentum diffusivity to thermal diffusivity
  • Determines ratio of fluid/thermal Boundary layer thickness
  • ${Pr}^{1/3} = \frac{δ_f}{δ_t}$



Grashof Number




$Gr = \frac{gβΔTL^3}{ν^2}$
  • Ratio of natural convection buoyancy force to viscous force
  • $\frac{Gr}{Re^2} << 1  \implies$ forced convection
  • $\frac{Gr}{Re^2} >> 1  \implies$ Natural convection
  • $\frac{Gr}{Re^2} ≈1  \implies$ mixed convection

Peclet Number


$Pe = Re*Pr = \frac{UL}{α}$
  • Ratio of convective to diffusive heat transport in a fluid
  • Used to determine plug flow/perfect mixing (CSTR) continuous flow model validity


Stanton Number


$St = \frac{h}{ρUC_p} = \frac{Nu}{Pe} = \frac{Nu}{RePr}$

  • Ratio of heat transferred to the fluid to the heat capacity of the fluid.
  • Used to characterize heat transfer in forced convection flows.

Rayleigh Number


$Ra = Gr*Pr = \frac{gβΔTL^3}{αν}$
  • It is product of Gr and Pr.
  • Determines natural convection boundary layer is laminar or turbulent.

Jakob Number


$Ja = \frac{C_p(T_s - T_{sat})}{h_{fg}}$
  • Ratio of sensible heat to latent heat absorbed (or released) during the phase change process.


Bond Number


$Bo = \frac{gL^2Δρ}{σ}$
  • Ratio of gravitational force to surface tension force
  • Used to characterize the shape of bubble or drops moving in a surrounding fluid. 


Froude Number

$Fr = \frac{U^2}{gL}$
  • Ratio of Inertia force to Gravitational force
  • Often the term Froude number is used for the ratio $\frac{u}{\sqrt{gL}}$.

Euler Number

$Eu = \frac{Δp}{ρU^2}$
  • Ratio of pressure force to inertia force.
  • Used for analyzing fluid flow dynamics problems in which the pressure difference, are interest

Weber number


$We = \frac{ρU^2L}{σ}$
  • Ratio of Inertia force to surface tension force.
  • Used for analyzing fluid flow dynamics problems in which surface tension is important

Nomenclature:


μ → viscosity of fluid
ν → kinematic viscosity of fluid 
ρ → density of fluid
U → characteristic velocity scale
D → characteristic Diameter = 4A/P
α → thermal diffusivity of fluid 
t  → time
L → characteristic length scale 
Cp → specific heat at constant pressure
h → heat transfer coefficient
K → thermal conductivity of fluid
Kf → thermal conductivity of fluid
Ks → thermal conductivity of solid 
g → gravitational acceleration 
β → volumetric thermal expansion coefficient 
ΔT → characteristic temperature difference 
Tsat → saturation temperature
Ts → surface temperature 
hfg → latent heat of condensation
Δρ → difference in density of the two phases 
σ   → surface tension
Δp → characteristic pressure difference of flow
δf  → Fluid boundary layer thickness
δ → Thermal boundary layer thickness



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