Page 311 - Chemical Process Equipment - Selection and Design

9.10. SPRAY DRYERS

Performance Data of Spray Dyers
[a) Daltia of KrOll (1978)
Moisture Air
Content Temperature
Spray Flow
Kind of Stock In(%) Out(%) Device Pattern In (“6) Out (“6)
Skim milk, d = 60 pm 48-55 4 wheel or parallel 250 95-100
50-60 4 nozzle
170-200 bar parallel 250 95-100
Whole miiik 50-60 2.5 wheel or
nozzle
100-140 bar parallel 170-200
Eggs, wh’ole 74-76 2-4 wheel or
nozzle parallel 140-200 50-80
Eggs, yolks 50-55 2-4 wheel or
nozzle parallel 140-200 50-80
Eggs, whites 87-90 7-9 wheel OF
nozzle parallel 740-200 50-80
Coffee, instant, 300 pm 75-a5 3-3.5 nozzle parallel 270 110
Tea, instaint 60 2 nozzle,
27 bar parallel 190-250
Tomatoes 65-75 3-3.5 wheel pa ral [el 140-150
Food yeast 76-78 8 wheel parallel 3 0 0 - 3 5 0 a 00
Tannin 50-55 4 wheel parallel 250 90
PVC emuision, 90% >80 pm 40-70 0.01-0.1 wheel or
<60pm nozzle or
pneumatic parallel 165-300
Melamine-urethane-formaldehyde resins 30-50 0 wheel
140-160 m/sec parallel 200-275 65-75
Heavy duty detergents 35-50 8-13 nozzle,
30-60 bar counter 350-400 90-130
Kaolin 35-40 1 wheel parallel 600 7 20

b) BerFormance of a ryer 181t Dia by left High with a Spray Wheel and a Fan Capacity of 11,000d
utiet6’
____~~
Air Temp (“F)
% Water Evaporation
Material In Out in Feed Rate ~l~/h~)
-~
Blood, animal 330 160 65 780
Yeast 440 140 86 1080
Zinc sulfate 620 230 55 1320
Lignin 400 195 63 910
Aluminum hydiroxide 600 130 93 2560
Silica gel 600 170 95 2225
Magnesium carbonate 600 120 92 2400
Tanning extracU 330 150 46 680
Coffee extract A 300 180 70 500
Coffee extract B 500 240 47 735
Magnesium chloride 810 305 53 1140
(to dihydrate)
Detergent A 450 250 50 660
Detergent B 460 240 63 820
Detergent C 450 250 40 340
Manganese sulfate 600 290 50 720
Aluminum sulfate 290 170 70 230
Urea resin A 500 180 60 505
Urea resin B 450 190 70 250
Sodium sulfide 440 150 50 270
Pigmeni 470 140 73 1750
aThe fan on this dryer handles about 11,00Ocuft/rnin at outlet conditions. The outlet-air temperature includes cold air
in-leakage, and the true temperature drop caused by evaporation must therefore be estimated from a heat balance.
(Bowen Engineering Inc.).