ALKALI - CHLORINE - SULFUR - BALANCE
Plant Date Time
Kiln Type, make Preheater / PC kiln Heat consumption kJ/kg cli
Length m Thermal load (BZ) 0.0 MW/m2 Clinker production t/d
Diameter (BZ) m Length of fix coating m 0.0 t/h
Cooler Type, make L coating / kiln diam.: 0.0 -
Cleaning method Obser- O2 kiln inlet %
frequency vations O2 PH outlet %
Fuels (sulfur input) Emission at main stack (including bypass stack)
Fuel type CV S Fineness Rate Heat SO2-Emission (sulfur output) HCl-Emission (chlorine output)
[kJ/kg] [%] [% 90mm] [t/h] [%] O2, at SO2 measurement %O2 O2, at HCl measurement %O2
0.0 Dry exh.gas at 0.0%O2 0.280 Nm3/kg cli Dry exh.gas at 0.0%O2 0.280 Nm3/kg cli
Main firing
0.0 SO2 dry ppm HCl dry ppm
0.0 SO2 0 mg /Nm3 HCl 0 mg /Nm3
0.0 0 mg/kg cli 0 mg/kg cli
0.0 0.0 kg SO2/h 0.0 kg HCl/h
Sec. Firing
0.0 SO3 0 mg/kg cli Cl 0 mg/kg cli
or PC
0.0 SO3 cli basis 0.000 % Cl cli basis 0.000 %
0.0
Calculated specific fuel cons. (from above data) 0 kJ/kg
Balance Massflow SO3 K2O Na2O Na2Oequiv Cl A/S Mass Balance
rate cli basis conc. cli basis conc. cli basis conc. cli basis cli basis conc. cli basis LOI cli basis
[t/h] [t/t cli] [%] [%] [%] [%] [%] [%] [%] [%] [%] [-] [%] [t/h]
1 Kiln Feed (dry) as fed 0.00 0.000 0.000 0.000 0.000 0.0000 0.0
2 0.00 0.000 0.000 0.000 0.000 0.0000 0.0
0.00 0.00 0.0
0.00 0.00 0.0
INPUT
0.00 0.00 0.0
0.00 0.00 0.0
3
0.00 0.00 0.0
0.00 0.00 0.0
0.00 0.00 0.0
0.00 0.00 0.0
TOTAL INPUT 0.000 0.000 0.000 0.000 0.0000 0.000 0.0
4 Clinker 0.00 0.00 0.000 0.000 0.000 0.000 0.0000 0.000 0.0
OUTPUT
5 Bypass dust removed from kiln 0.00 0.000 0.000 0.000 0.000 0.0000 0.0
6a Dust (main filter) returned via kiln feed 0.00 0.000 0.000 0.000 0.000 0.0000 0.0
7 Dust (main filter) removed from kiln 0.00 0.000 0.000 0.000 0.000 0.0000 0.0
8 Emission - - 0.000 - - - - - - 0.0000 - - -
TOTAL OUTPUT 0.000 0.000 0.000 0.000 0.0000 0.000 0.0
Input - output 0.000 0.000 0.000 0.000 0.000 0.00
Diff.
in % of input 0.0 0.0 0.0 0.0 0.0 0.0
(red values: estimated figures)
Hot meal Massflow SO3 K2O Na2O Na2Oequiv Cl A/S Mass Balance
conc. Limits conc. conc. conc. Limits conc. Limits LOI Calcination
[%] [%] [%] [%] [%] [%] [%] [%] [%] [%]
Mix right + left - 0.000 - - -
437656658.xls HGRS/CTS/TPT 09/16/2019
- - - -
Average 0.000 0.000 0.000 0.000 0.000 0.000 0.0
437656658.xls HGRS/CTS/TPT 09/16/2019
Applicable Balance Boundary for all Kiln Types:
437656658.xls HGRS/CTS/TPT 09/16/2019
EVALUATION of ALKALI - CHLORINE - SULFUR - BALANCE
- The following section is only applicable if the balance boundary as shown on the balance sheet is used
(balance boundary excluding outer dust cycle).
- For additional information and explanations see 'Manual Alk/SO3/Cl - Balance"
Main Results: HGRS criteria for Preheater / PC kiln :
1. "Calculated" Cl in clinker*/**: n/a g/t cli < 200-300 for all kilns
2. Actual Sulfur in clinker: n/a %SO3cli < 1.5
3. Alk/SO3 ratio in clinker: n/a - 0.8 - 1.2
4. "Relevant" Cl input***: n/a g/t cli < 300 (no Cl valve)
5. Sulfur Volatility #DIV/0! - <0.7
6. Hot Meal: see graph below
* "Calculated" value in clinker = Total inputs minus dust output and emission, referred to clinker.
** "calculated" CL value shows more reliable values than the real value in clinker (which is heavily depending
on the current circulation situation)
*** "Relevant Input= All Cl inputs minus Cl in dust reused (via kiln feed or returned directly) in the kiln process minus emission
Limiting criteria HGRS: Maximum possible Cl input when maximising Cl valves
Note: The Chlorine limit of 5000 g/t clinker for wet/long dry kilns is from the process point of view only.
If all dust goes to the cement, the chlorine limit is usually around 1000 gr/t clinker.
Hot Meal Evaluation for SP/PC Kilns
2.400 frequent
blockages
2.200
2.000
1.800
1.600
% Cl
1.400
1.200
1.000
0.800
0.600
0.400
0.200
0.000
0.000 0.500 1.000 1.500 2.000 2.500 3.000 3.500 4.000 4.500 5.000 5.500 6.000
% SO3
437656658.xls HGRS/CTS/TPT 09/16/2019
