567128122-Raw-Meal-Clinker-Quality-Control.ppt

Adjust raw material

2. MUGHER CEMENT ENTERPRISE
Raw Meal & Clinker Quality Control

3. Module Objectives
What is the goal of clinker burning?
What are the testing techniques in cement
industries?
What are the cement manufacturing
process’s variables and factors?

What are the objectives of raw meal
control?
How to calculate raw mix composition?

4. Module Objectives(Continue)
What is the role of raw meal fineness and
particle size distribution?
What is the importance of raw meal
homogeneity?
What are the reactions during
clinkerization?
What are the objectives of clinker control?

5. Module Objectives(Continue)
What are operational measurements on clinker?

What are the factors that affects the correlation
between raw meal and clinker composition?
What is the need of clinker cooling?
 What are cement plant control (follow-up)
parameters?

6. Definition of Cement
Ordinary Portland Cement (OPC):
Portland cement is the finely ground
clinker with some gypsum added.

Pozzolanic Portland Cement (PPC):
Pozzolanic Portland Cement is the finely
ground clinker with some pozzolana
(pumice) & gypsum added.

7. Portland Cement Clinker
The manufacturing of clinker involves
the conversion, at high temperature of
mineral mixtures of natural origin, into
new mineral mixtures which have
hydraulic properties.
It is an intimate mixture of: Calcareous
materials (CaCO3), Argillaceous, Silica ,
Alumina, Iron Oxide.

8. “Heating of the raw
meal to the required
temperature so as to
produce the desired
clinker compounds in an
economic way at higher
productivity in the
preheater & kiln.”
Pyro processing

9. What is the goal of clinker
burning?
The production of
GOOD QUALITY
cement

10. What is cement quality?
Cement quality is defined in terms of
characteristics & properties such as:
Chemical composition (Oxides content limits)
Physical properties (Strength, Workability,
Setting behavior etc) in Standard Norms
(ASTM, ISO) and is measured used standard
methods

11. To many people who make and
market cement, 'quality’ means
conforming to the standards,
codes and manuals
established in accordance with
the modern quality conformity
industry

12. Factors influencing cement quality
Chemical & mineralogical
composition of clinker
Additives Quality such as Gypsum,
Pozzolana
Mechanical handling of clinker
(grinding)

13. Production of Good quality clinker from the kiln
depends on :
 Good raw mix design which in turn depends on
1.Desired clinker minerals
2. Allowable free lime
3. Nature of the raw material
 Liquid ratio & Residence time in the kiln
 Fuel quality & Combustion
Burning process
Fineness of the raw meal to the desired level
Circulation phenomena

14. Quality Control

15. Quality control concepts
A detailed control plan for quality control of each
raw material, intermediate & final product is
setup by a thorough analysis of the following
questionnaire.
What should be examined?
What information is required for the control?
How often must the test be performed?
How accurate must the result of the testing be?
 

16. What is sampling?
Sampling is the process to collect a representative
& sufficient quantity of material (sample) to be
analysed.
Generally there are two types of samples
1.Spot sample:
samples that is collected at a certain moment or the
portion taken from the collected material (i.e. un-
homogenized).
2. Representative sample:
samples that represent the full quantity
or a full period of time.

17. Are auto samples always representative?
The collection of the sample must be
continuous to ensure representative
auto sampling

18. Consequence of wrong sampling
& wrong analysis
1.Wrong sample + correct analysis =
Wrong action
2. Correct sample+ Wrong analysis =
Wrong action
3. Correct sample + Correct analysis =
Right action

19. Common Testing Methods/techniques in
cement industry
1.Chemical composition (Complete analysis ):
Complexometric titration and/or X-ray
Fluorescence
2.CaCO3 : Carbonate titration (back titration) &
Prompt gamma neutron activation technology
(PGNAA)
3.Fineness : Sieving @ different mesh size
4.SO3: Gravimetric, X-ray Fluorescence & LECO
Sulpure analyzer

20. Common Testing Methods/techniques in
cement industry (continue)
5.Alkalies (K2O & Na2O): Flame photometer,
atomic absorption spectroscopy (AAS) & X-ray
Fluorescence
6.Chlorine: Potentiometeric titration, X-ray
Fluorescence
7.Loss on ignition(LOI): Ignition the sample in
Laboratory muffle furnace @ 1000
0
C
& LOI analysis
instrument
8.Free lime(uncombined CaO) :Titration(ethylene
glycol method), conductometric (Automatic free
lime analyzers) & X-ray diffraction

21. Material
Burnability

22. Material burnability
The readiness with which a raw mix is
transformed into clinker minerals in the
course of high temperature treatment
 Arranged as easy, normal, or difficult to
burn
There is interrelationship between feed meal
burn-ability and clinkering process
properties such as: residence time,
maximum temperature and pressure, and
cooling rate

23. Reactivity & burnability of Raw
Mix
Reactivity and burnability are properties
which affect the plant capacity and the
process thermal consumption, because
raw meal sintering is considerably altered
by such factors

24. Reactivity & burnability of Raw
Mix(continues)
Reactivity is related to the rate of
reaction for certain conditions and
temperatures
Burnability expresses the difficulty
for the material to be converted at
any time, in the process temperature

25. Reactivity & burnability of Raw
Mix(continues)
Reactivity and LSF affect the
burnability value, since reactivity is
a function of the Silica Ratio (SR),
Alumina Ratio (AR), granulometry ,
present mineralogical species and
their chemical activity

26. Factors influencing the reactivity
1. The raw mix preparation
Chemical factor …………… SM,AM
Granulometric factor ……Fineness and
Particle size distribution (PSD)
2. Inherent characteristics of raw
materials( The intrinsic reactivity of the
raw materials), which can not be
modified:

27. Factors influencing the reactivity
(continues)
Different raw mix with the same chemical
composition and equal fineness may differ
in their burnability due to their different
mineralogical composition
Some types of silica ,for example, will react
more readily than will other
Quartz
Silica sand

28. Factors influencing the reactivity
(continues)
Other examples of mineralogical property
Calcite (CaCO3) crystals
Rhombic
Cubic
Clay
Caolinit
Kaolinit (A
14
(OH)
8
Si
4
O
10
)

29. Flux & Mineraliser
Desired Clinker Quality
Mineralogy of Raw meal
Chemical Composition
Fineness
% Liquid
Clinker Burnability factors
(Summary)

30. Raw meal
Control

31. Purpose of raw material
preparation
Control of the materials composition prior
to excavation enables selective quarrying
to achieve.
Correct composition of (integrated) stock
piles
Medium to long term uniformity of stock
pile composition
Optimum utilization of materials and
equipment

32. Raw mix control
Raw mix preparation is the quality key
control parameter upstream for stable,
continuous manufacture of high quality
clinker and cement
Raw mix control aims for the lowest
possible deviations from the quality
targets at the conveyor belts, the mill
and homogenization silos

33. Raw meal control objectives
Blending of components to obtain the
target composition of raw meal and
clinker
Achievement of target meal fineness to
obtain appropriate clinker burnability
Achievement of a sufficient uniformity
which, together with the homogenization
in the subsequent silo, results in a high
kiln feed uniformity

34. Raw mill control
Mill % ball charging
Mill speed
Adjustment of feed proportion to the mill
(Raw mix design)
Materials flow rates(Feed rate control)
Materials bed thickness (for VRM)
Air flow rates (Air /gas quantity control)
Air / gas temperature control

35. Raw mill control(continues)
Pressure inside the mill
Re-circulation rate
Separator speed
Raw meal fineness control
Raw meal composition control
Ref : Page 8 – 11 & 45

36. Raw Mix
Design

37. Objectives of proper raw mix design
Obtain good quality clinker with
minimum free lime
Obtain suitable liquid phase to carry the
reactants ( good reaction)
Build up optimum coating to elongate
the refractory life time
Minimize the fuel consumption (cost
factor)
Suitable smooth operation of kilns

38. Raw mix design parameters
The proportioning of raw mixes for
Ordinary Portland cement is mostly
based on the following specific criteria:
Lime saturation factor (LSF)
Silica Ratio (SR)
Alumina Ratio (AR)

39. Lime saturation factor (LSF)
The amount of CaO which is enough to
saturate or combine SiO
2, Al
2O
3, and Fe
2O
3 to
form Portland cement clinker
LSF= [CaO / (2.8SiO
2+1.2Al
2O
3+0.65Fe
2O
3)]*100
Desired value 92-98 %

40. Effect of high LSF
Difficult to combine with other oxides
(hard to burn)…. A tendency to high free
lime
Fuel consumption increases
Burning zone temperature increases and
heat loss by radiation increases
Brick life will be short
Presence of Free CaO affects the quality of
clinker and produces unsound cement

41. Effect of low LSF
Free lime content is usually low…Form less
porous & bally clinker ….. Results, hard to
grind
Excess of liquid phase in the burning Zone,
there is a tendency to ring formation and
coating washing
The potential C
3S is lowered and the C
2S is
increased proportionally……Reduce early
strength of cement

42. Silica Ratio (SR)
The silica ratio establishes the relation
between silica, alumina and iron; so
that the right amounts of the
aluminates C
3
A and Ferrite C
4
AF are
obtained in the clinker.
SR= SiO
2/ (Al
2O
3+Fe
2O
3)
 Desired value 2.0 - 2.4

43. Effect of high silica ratio (SR)
Difficult to combine with CaO …hard to
burn
More fuel consumption
High heat loss by radiation
Reduces the amount of coating in the
burning zone
Produces dusty clinker

44. How high SR values decrease
burnability ?
Increased probability of having big SiO2
particles in raw meal
Decreased amount of clinker melt
A tendency for decreased homogeneity
of raw meal (segregation)
Ref : page 15,

45. Liquid phase
Part of kiln feed which melts in the kiln
Vital in that it acts a flux ,promoting
reactions by ion transfer ,with out the
liquid phase ,combinability would be poor
and it would be very difficult to make
clinker
Composed largely of oxides of calcium, iron
and aluminium, with some silicon and other
minor elements (Magnesium, Alkalies)

46. Effect of low silica ratio (SR)
Excessive coating formation (ring
formation)
Fast brick infiltration with clinker melt
Snowman formation in cooler
Shark teeth(Stalagmite & stalasite)build-
up at the nose ring
Resulting bally clinker which is hard to
grind and its strengths are lowered

47. Relationship of Silica Ratio Vs
Lime Saturation Factor on
burnability
As both the LSF and SR are increased, the
mix becomes harder and harder to burn
and coating tends to disappear. If both
modules are reduced at the same time,
the raw mix becomes easier and easier to
burn and brick wash outs are most likely
to occur
Ref : page 15 - 16

48. Alumina Ratio (AR)
The Alumina ratio establishes the
relation between alumina and iron to
determine the viscosity of liquid phase
AR= Al
2O
3/Fe
2O
3
Desired value 1.4 – 1.60

49. Effect of high Alumina ratio
1.The more viscous flux at a given
temperatures
Decrease sintering rate due to decrease
in reactant contact (decreases the kinetic
energy of the reactants)
 Increase sintering temperature to make
less viscous ( to increase sintering rate)
• High fuel consumption to increase
sintering temperature

50. Effect of high Alumina
ratio(continues)
2. High C3A formation
High heat of hydration (Reaction of C3A
with water releases 900KCal energy per
mole of C3A)…… Results concrete thermal
expansion
 Tendency to high early strength due to
high heat of hydration , consequently it
absorbs high amount of water for
quenching

51. Effect of low Alumina ratio
Means high Fe2O3 content (less viscous
clinker melt )
Hard to grind due to formation of less
porous clinker
Form Dark in color of clinker

52. Purpose of calculating the
composition of the raw mix

To determine the quantitative
proportions of the raw components,
in order to give the desired chemical
and mineralogical composition of
the clinker at minimum cost

53. Mix design requirements
It the cardinal rule that the number of
target that can simultaneously be met in
any mix design is equal to the number of
raw components minus one
At least one raw material must have a
value any parameter higher than the
target ,& at least one material must a
value below the target value

54. Methods for Calculating the Raw mix
Proportioning (Ref : Page 17 – 21)
A)Two component system
 Blending Rule (X-pattern)
 Based on lime saturation factor (LSF)
B) Three component system
Based on Lime Saturation Factor and Silica Ratio
C. Four component system
Based on LSF, SR and Alumina ratio(AR)
D) N - component system (n >1 )
Based on minimum cost with computer
application (E.g Excel solver & Other computer
soft wares)

55. Raw meal
fineness

56. Raw meal fineness
 The rates at which reactions take place are
generally depend on the particle size of the
reactants (CaO,SiO2,Al2O3,Fe2O3)
Fine material will evidently react more
readily than will coarser material, so finer
material makes of better combinability
Optimum value 12-14 % @ 90 µm Sieve
residue

57. Advantages of increasing raw
meal fineness
Shorter time required for preheating of
suspended raw meal in preheater
 Faster calcination and clinkerization
reactions
 Increase in clinker production rate
 Reduction in specific fuel consumption

58. Disadvantages of increasing the
raw meal fineness
Increase in specific power
consumption of raw mix grinding
Loss of material in the form of
dust

59. Effect of coarse grains
Studied with optical microscope
Coarse quartz and calcite results in poor burnability,
high free lime and too little C
3S in the
clinker…..Reduce strength
Critical size of particle for residual free lime after 30
minutes
Quartz - 45 microns
Calcite - 125 microns
1% increase of
Quartz
+45mic
----> 0.93% Free CaO
Calcite
+125mic ----> 0.93% Free

60. Particle Size Distribution(PSD) of
raw meal
The mix having lower fine fraction &
higher average particle size is poor in
burning (Burnability depends on PSD)
Recent studies have demonstrated that
PSD of the raw meal plays a major
decisive role than the simple fineness in
determine in pyroprocessing & final
material characteristics

61. Raw Meal
Homogenization

62. Raw meal homogenization
The basic principle of blending process is one or
combination of the following mechanisms.
Distribution of input raw meal at the blending silo
top
Pneumatic dry blending by aeration of raw meal
by the aeration units placed at the bottom of silo
Segmental aeration (octant or quadrant system)
with difference in the pressure of air supplied for
aeration of various segments for thorough mixing
of raw mix

63. Homogeneity and burnability
Insufficient control of the raw mixture and
its blending will cause large variations in the
chemical composition of the kiln feed
(fluctuations in product quality)
If the kiln is operated at a constant material
residence time and temperature, such
variations also will cause variations in clinker
composition, including free lime

64. Homogeneity and burnability
(continues)
When unintended variation in kiln feed
composition causes large variation in
free lime, operators may make incorrect
changes to kiln operation, assuming
changes are needed when they are not

65. Homogeneity and burnability
(continues)
The operator may be obliged to increase the
burning zone temperature to achieve the
desired free lime level — by keeping the kiln on
the hot side, the maximum clinker free lime is
brought to the average value. Results reduced
brick life time
The fuel penalty for burning to an average of
0.8% free lime because of large variability
instead of an average of 1% can easily be on the
order of 4% (high fuel consumption)

66. Homogeneity and burnability
(continues)
When the kiln is operated on the hot side, alkalis
and sulfate become more volatile. This, in turn,
might increase the possibility for build-ups in the
heater & Kiln inlet (increased tendency to ring and
build up formation
Hard burning tends to cause low clinker porosity,
large crystals of alite, and often contributes to
generation of dust instead of good, nodular clinker

67. Homogeneity and burnability
(continues)
Slows down the cooling process, both
because of high temperature and low-
porous clinker is more difficult to cool.
Reduced clinker porosity can make the
clinker harder to grind, increasing finish
mill power consumption or reducing
mill production
Reduced cement strength potential

68. Blending Factor
The ratio of standard deviation of input raw
meal to standard deviation of output raw
meal
 The standard deviation is a measure of how
widely values are dispersed from the average
value (the mean)
For calculation of blending factor of a silo,
input and output raw meal samples are to be
collected in regular intervals and to be tested
for example CaCO3 content

69. Blending Factor(continues)
STDEV uses the following formula
where x is the sample mean
AVERAGE(number1,number2,…) and n is the
sample size.
There are various types blending silos having
blending factor from 6:1 to 15:1
The more the blending factor, the blending is
more effective

70. Kiln Feed
Control

71. Kiln feed control
Provides guide line information (LSF,SR,AM)
for kiln operation on currently processed
material as well as indications on the raw
material blending and homogenizing
efficiency

72. Sources of kiln feed fluctuations
Raw components: chemical and
mineralogical composition & inherent
characteristic
Raw meal : chemical and mineralogical
composition, Fineness, disturbances in feed
rate to the mill.
Combustible : ash content, sulphur content,
calorific value, fineness

73. Sources of kiln feed fluctuations
(continues)
Dust return: different modes of return
during direct or indirect operation
Feed rates: equipment related fluctuations
at constant (kiln feed, combustibles) settings.
Abrupt manual adjustment of kiln operation
parameters
E.g : Sourse of kiln meal CaCO3 variation
Ref : Page 47

74. Means of improving uniformity
 The kiln feed uniformity is a result of
various factors along the preparation
process, starting from the raw material
deposits and going through several stages of
homogenization and blending
Exploitation planning
Medium to long term exploitation planning,
based on accurate raw materials inventory

75. Means of improving uniformity
(continues)
Quarry scheduling
Short term quarry scheduling, based on
blast hole dust analysis
Blending control
Blending control at integrated pre-blending
stock pile
Raw meal control
Raw meal homogenization control

76. Hot Meal
Control

77. Hot meal control
Determination of concentration of volatile
elements(SO3,Alkalies,chlorine) in the case
of kiln systems affected by build up
formation in the preheaters and/or kiln
inlet area
Determination of non-burnt combustibles
introduced with the kiln feed or the
secondary firing (pre-calciner)
Determination of the degree of pre-
calcination

78. Volatile Matters present
SO
3
Cl
K
2
O
F
OH
Na
2
O

79. Circulation of volatile matter
A fraction of the volatile components evaporates in the
kiln burning zone and condense in the back end or raw
meal and re-enter the burning zone
The repeated evaporation and condensation results in
an Internal circulation where the concentration can go
up to fifty times the input concentration
At equilibrium state, the output of volatiles along with
clinker is equal to the total input from raw meal and
fuel
Higher degree of volatiles concentration exists either
due to more input or due to a high degree of volatility
(high burning)

80. External circulation
Volatile matter in raw meal like sulfur, is
burnt to SO
2 gas in the preheater upper
cyclones at around 400 - 600 deg C and
expelled out from preheater but effectively
precipitated in Electro Static Precipitator
(ESP)

81. Condensation of volatile matter
Volatile matter with low melting point
condenses in preheater walls and raw
meal particles causing build ups on
cyclone
SO
2
gas combines with calcined raw meal
and condenses as CaSO
4
CaO + SO
2 + 1/2 O
2 --------> CaSO
4

82. Operational Aspects of Volatile
Components
Formation of build-ups in preheater riser
pipes and cyclones reduces the air volume
Reduced kiln production and increased
circulation of sulfur compounds due to less
availability of excess oxygen
Higher heat consumption
Dusty (unsintered) clinker formation

83. Normal
Limits
Max
Limits
K
2
O
eq
=K
2
O+1.5Na
2
O3.70% 6%
Chlorine as Cl
-
0.80%2.00%
Sulfur as SO
3 2.50% 5%
Limits On Volatile Components In Bottom Cyclone
Stage in a SP kiln system on LOI free Basis
CONTROL LIMITS

84. Normal
Limits
Max
Limits
K
2
O+0.65*Na
2
O 1.00% 1.5%
Chlorine as Cl
-
0.02%0.02%
Sulfur as SO
3 1.00% 1.6%
Max Allowable Input of Volatile Components for a
SP kiln system Without bypass on LOI free Basis
CONTROL LIMITS

85. Normal
Limits
Max
Limits
K
2
O+0.65*Na
2
O 1.00% 1.5%
Chlorine as Cl
-
0.015% 0.015%
Sulfur as SO
3 0.80% 1.2%
Max Allowable Input of VC for a CALCINER Kiln
system Without bypass on LOI free Basis
CONTROL LIMITS

86. Hot meal process interaction
The level of volatile elements indicate
changes in the absolute and relative input
of circulation elements with raw meal and
fuel, and corrective actions can-if possible-
be initiated
Improving combustion efficiency of
precalciner and consequently maintain the
appropriate hot meal degree of calcination
before entering to kiln

87. Raw mix control
SO
3 / Alkali ratio
Kiln by pass
Excess air
Flame adjustments
Reducing
Evop factor
Volatiles
Control
Methods
Discard the filter dust

88. Calcination Degree Determination
Calcination degree ( %) = 10000 (LOI
kiln meal – LOI
sample)
LOI
kiln meal (100-LOI
sample)

89. Clinker
Formation

90. Natural minerals Hydraulic mixture
Temperature
Time, Pressure

91. Kiln temperature Zones
Zone Temp(in Deg. C)
Drying Zone up to 120
Preheating Zone 100-150
Calcination Zone 550-1100
Sintering or Burning Zone 1100-1450
Cooling Zone 1450-1250

94. Clinker-reactions in the kiln

95. Clinker-reactions in the kiln cont.

96. Temperature
0
c

Chemical Process

Chemical transformation
200 -100
0
c Escape of free water None
100-400
0
c Escape of adsorbed water None
400-750
0
c
Decomposition of clay with formation of
meta kaolinate
Al
4
(OH)
8
Si
4
O
10
---------->
2(Al
2O
3.SiO
2) +H
2O
600-900
0
c
Decomposition of meta kaolinate & other
compounds
Al
2O
3.SiO
2 ---------> Al
2O
3+ SiO
2
600-1000
0
c
Decomposition of lime stone and formation
CS and CA
CaCO
3 ------>CaO+CO
2
CaO+ Al
2O
3 +
3 CaO+2 SiO
2
+ Al
2
O
3
-----> 2(CaO.
SiO
2
)+ CaO+ Al
2
O
3
800-1300
0
c
Up take of lime by CS &CA ; and up take of
F by the compounds formed to form C
2
S,C
3
A
and C
4
AF
CS+C -----> C
2
S
2C+S------> C
2S
CA+2C------>C
3
A
CA+3C+F-----> C
4
AF
1250-1450
0
c Up take of lime by C
2S to form C
3S C
2S+C---rev--> C
3S

97. 2.Decomposition rate of
limestone
Decomposition rate of limestone is increased
by :
Increase in temperature of raw meal
Lowering CO2 partial pressure in combustion
gases ….To prevent reverse reaction
Lowering dust load of combustion gases
Decreasing crystal content of CaCO3
High heating rate (E.g lower rpm of kiln , High
fuel rate ,installing precalciner)

98. Role of Precalciner (PC)
Around 90% of calcination is completed in
the precalciner
Precalciner reduces the thermal loading of
kiln and there by the length of the kiln.
The time taken by the raw meal to cross the
PC is called the residence time
.
Higher the residence time, higher will be the
time available for the degree of completion
of calcination reaction

99. Melt formation
Raw meal melts at more than 1200 deg C
depending on the amount of fluxing material
Liquid formation is important for
 Effective Granulation
 Stable coating
 Protecting the refractory

100. Melt formation (continues)
Raw mix composition determines the
 temperature of initial liquid formation
 the amount of liquid formation
 physical properties of the liquid such as its
viscosity
Fluxes(Al , Fe , Ba , Sr , Ce , Cr, P , Ti, Zn)
Lower melting temperature and melt
viscosity

101. Melt formation(continues)
A mineraliser like Fluorides(CaF2,NaF,BaF
MgF2)can also be added to reduce the
temperature at which liquid phase is formed
Mineraliser modifies the viscosity and
surface tension of the clinker liquid to
promote the formation of clinker minerals

102. Alite formation
Liquid phase
CaO + 2CaO.SiO
2
-------------> 3CaO . SiO
2
t >1250 C
3
S (Solid)
Formation starts at 1250 degC as C
3S and free
lime are only available as “Solid particles” in
kiln Charge
In the presence of liquid phase CaO and C
2
S
are dissolved and C
3S is formed
When the temperature reaches 1450degC, in
the solid phase C
2S, C
3S and a little free lime
only will be available

103. Reaction Equilibria
Belite + CaO Alite
Shift in reaction equilibria by changes in:
Temperature (+R;-L)
Quantity of melt ((+R; -L)

Melt viscosity (+L; -R)

Heating Rate between 1200-1450 °C (+R; -L)

Clinker cooling rate1450-1200 °C (+eq. “Freezes”-L)

104. Reactions during cooling
Rate of cooling is a critical parameter
Slow cooling results in decomposition of C
3
S
back to C
2S and consequently results in
* Reduced cement strength
* Poor grindability
Cooling process influences the state of
crystallisation and hence the reactivity of
clinker
The maximum rate of decomposition occurs at
1175 degC

105. Advantages of rapid cooling
Rapid cooled clinker will have
* The same composition as it had around
the clinkerisation temperature
* Improved Grindability
* Lower proportion of decomposed alite
and consequently a higher proportion of
alite in the clinker

106. Clinker Nodulization
Poor granulometry and Dusty Clinker leads to:
More wear rate in cooler and need more
maintenance
Formation of unstable, porous coating instead of
dense, stable coating
Poor grindability of clinker
Problematic clinker handling and dust nuisance
Unstable kiln operation

107. Clinker Nodulization(continues)
Particles are held together by capillary forces
of the liquid
Nodulisation depends on the amount of
liquid, particle size and the speed of the kiln

108. Clinker Nodulization(continues)
Formed C
3S crystals sinter together to form
coarse C
3S particles and slow down the
nodulisation process
Nodulisation is enhanced by liquid phase and
counteracted by large C
3S particles.
At higher BZ temp, the formation of C
3S
particles is faster and hence smaller will be
the nodule size

109. Reducing the Alumina / Iron ratio (1.4 - 1.6)
will improve the nodulisation as the
formation of liquid phase starts at lower
temperature
Lowering of the silica modulus increases the
amount of liquid and thereby improves the
nodulisation
Reducing the LSF reduce the potential C
3S and
thus increase the nodulisation
CHANGES IN CHEMISTRY &
CLINKER NODULISATION

110. Nodulisation
N
Amount of
C
3S
% Liquid
Length of
burning
zone
Particle
size
Temperature
Residence
time

111. Operational measurements on
Clinker
1.Litre Weight of clinker
It is usually of 5-10mm or 6-12mm particles
that are sieved and weighed in a cup with
fixed volume.
The top of the cup is leveled with a ruler. The
measurement in g/lt is generally between
1100-1300 (desired value 1250-1350)

112. Operational measurements on
Clinker (continues)
The litre weight of a clinker type at a
specific plant correlates to the free lime
when burnability remains constant.
Higher temperature generally gives higher
litre weight but very high temperatures
can lower the litre weight because of dust
agglomerates.

113. Operational measurements on
Clinker (continues)
2. Free Lime ( Uncombined CaO )
The primary criteria of clinker
quality. This is because
 Too high free lime: Loss in
strength potential, increase of
cement expansion, disturbances in
cement grinding

114. Operational measurements on
Clinker (continues)

Too low free lime : Loss in cement
reactivity, excessive heat consumption,
poor grindability
The free lime measurement to be
carried out on a representative sample
of the clinker product. Generally the
free lime is targeted just below 1.5%.

115. Operational measurements on
Clinker (continues)
Composition, temperature, residence
time & burnability influence the
achieved free lime level.

116. CORRELATION BETWEEN FREE
LIME CONTENT & LITERWEIGHT
Generally CaO
free inversely to liter
weight at a given SM
But there is loss of such correlation
between Free lime content and
Liter weight for over burnt clinker
Ref : Page 34

117. Kiln process variables ,control &
interaction
Air flow rates ( by ID fan Speed & cooler fans)
 primary air
Secondary air
Tertiary air
Flame Characteristics (by air , fuel rate &
burner position)
Flame temperature
Flame length
Flame stability

118. Kiln process variables ,control &
interaction(continues)
Residence time of kiln meal with in the
kiln (kiln speed)
Chemical composition, parameters and
minerals of clinker (By Analysis)
Volatile concentration(By analysis)

119. What are the factors that
affects the correlation
between raw meal and
clinker composition?
Ref : Page 38 & give
comment

120. Factors that affects the correlation
between raw meal and clinker
composition
It is known that the set points of the raw
meal composition have to be such that the
target composition of the clinker is being
obtained. Allowance has there fore, to be
made for:
The kiln dust absorption in the raw mill( kiln
dust composition can significantly deviate
from the kiln feed composition)

121. Factors that affects the correlation
between raw meal and clinker
composition(continues)
The discarding of the kiln dust …..Loss
Systematic errors in sampling and analysis
The primary target is the clinker
composition. If any of the above factors
change, the raw meal set point has to be
adjusted accordingly

122. Varieties of Dust
The following varieties of dust are
generated in the operation of cement
Raw materials & additives dust
Raw mix dust
Coal dust
Exit dust from kilns
Clinker dust
Cement dust

123. Varieties of Dust(Continues)
With the exception of the kiln dust ,the
kinds of dust enumerated above, show the
same chemical composition as the original
material
The kiln exit dust represents a mixture of
raw mix and clinker ;the chemical
composition of the kiln exit dust is among
other factors also influenced by the size of
the particles carried away by the kiln gases

124. Example of ESP dust composition
CaOSiO2Al2O3Fe2O3MgO LOIMoist
ure
47.197.464.031.811.2736.940.60

125. Clinker
Cooling

126. Purpose of clinker cooler
To cool the Clinker

127. Importance of clinker cooling
1.From engineering view point, to prevent
damage to clinker handling equipment
such as conveyors
2.From process view point, it is beneficial
to minimize clinker temperature as it
enters the cement mill to prevent
dehydration of gypsum(formation of
plaster of paris) in cement
mill…..Regulate setting time

128. Importance of clinker cooling
(continues)
3.From an environmental & a cost view point,
reduces energy consumption by extracting heat
from the clinker ,enabling it to be used to heat
the raw mix and secondary air & tertiary air
required for fuel combustion
4.From a cement performance view point, faster
cooling of the clinker enhances silicate reactivity
& improve grindability due to the presence of
microcracks in alite & due to the finer crystal size
of the flux phases

129. Importance of clinker cooling
(continues)
Resistance to chemical attack
C3A content, which is related to the
resistance of Portland cement to attack
by sulfate solution, is mainly present in
the glassy state, when cooled rapidly. In
this form C3A is much less susceptible to
attack by sodium or magnesium sulphate

130. Cooler Process variables &
interaction
Cooler speed
Materials bed thickness (Grate cooler)
FD fans speed (Grate cooler)

131. Cement Plant Control (follow-up)
parameters
Ref : Page 39 - 44
Lime Saturation Factor (LSF)
Silica Ratio (SR)
Alumina Iron Ratio (AR)
% Liquid phase at the burning zone (Lph)
Coating index (CI)
Minimum Burning temperature
0
C

132. Cement Plant Control (follow-up)
parameters(continues)
Burnability index (BI)
Burnability Factor (BF)
Alkalis Equivalent
Alkali sulphate Ratio (ASR)
 Sulphate Modulus (Mso
3
)
Bogue’s potential composition
Homogenity of the process

133. Productivity
Productivity=Actual
production/Maximum production
Acceptable approximate level > 0.8
 
Productivity is a measure of the
following:
System performance
System efficiency
 

134. Productivity(continues)
Resource utilization
The relationship between real output and inputs.
Productivity is measured as:
The ratio of output to input
The ratio between the amount produced and the
amount of any resources used in the production
Output per unit of input (resources)
 

135. Productivity(continues)
Nowadays the challenge is to change the
cement industry from traditional mass
production into more effective production
system aiming to increase the productivity,
overall performance, and capacity utilisation
to meet high market demand. The cement
industry is forced to reduce the production
costs and delay times in order to take
advantages in the global competition
environments.

136. Process Optimization
Within the cement production line, Process
Optimation (an effective tool for cost
reduction) is an initiative to improve the
plant performance
The objectives for Process optimization
include:
Optimization of all unit operations
Lowering the specific energy consumption

137. Process Optimization(continues)
Diagnostic studies of problems in raw
materials, electrical, instrumentation,
mechanical and process engineering
sections and trouble shooting
Quality assurance with optimized
utilization of resources
Measures for improvement in
environment
Lowering the production cost

138. Conclusion
In current scenario of limited demand,
lower cost realization and increasing
competition in cement industry, lowering
the production cost has become the
need of the hour for survival. An
effective measure to reduce the
production cost is by optimization of the
operational practices