298 94 307/02 Untersuchungen zum Stand der Umsetzung des ...
298 94 307/02 Untersuchungen zum Stand der Umsetzung des ... 298 94 307/02 Untersuchungen zum Stand der Umsetzung des ...
- thermal - catalytic • Biological separation - Bio-filter - Bio-purification 4.6.1 Bio-filter technique Description Teil 3 Seite 4-57 By means of the planned new plant, odour laden exhaust air from machines and proc- essing plants, as well as chamber air from operational chambers is to be captured and channelled into a biofilter via a pipeline system in order to reduce emissions. In total, 100.000 rn3/h of exhaust air is to be captured and treated. Achieved environmental benefits Cross media effects The water seeping through the filter bed is collected under the slatted floor and chan- nelled into the sewage system through a drain. Concrete details regarding the volumes involved are not possible. In any case, however, the volume of seepage water is exclu- sively dependent on the precipitation volume and is significantly lower than this. Operational data Applicability Economics operating time: 5000 h/a 1. energy consumption: 40 % part load) 2 exhaust fans each with 58 kW * 3.000 h/a * 0,065 €/kWh = 22.620 € 2 exhaust fans each with 23 kW * 2.000 h/a * 0,065 €/kWh = 5.980 € 2 circulating pump for the scrubber = 4875 € 2. Water consumption, condensate disposal pors. 60 % full load exhaust vapors: 0,28 t/t fish converting * 15 t fish / h makes 3,87 t/h exhaust va- 60 % into waste water treatment plant, 40 % evaporation = 2,32 t/h exhaust vapors 0,68 t/h washing wate summation= 33.475 € 3 t/h * 2,6 € (WWTP)/m³ summation=39.000€/a
Teil 3 Seite 4-58 3. Filtermaterial: exchange each 4 year summation= 14.000 €/a 4. Maintenanance summation=7.000 €/a 5. Cost of operation (summation Nr. 1 - Nr. 4) 93.475 €/a Driving force for implementation Example plants Example plant: Vereinigte Fischmehlwerke Cuxhafen GmbH & Co KG, Germany At this plant, exhaust air from the sectors: Boiling apparatuses Pre-sifting Presses Decanters Dryers Centrifuges Concentration plant is treated. Since the exhaust air still has a considerable heat content, the intention is to utilise a portion of this heat during the new pre-concentration. I.e. the exhaust air of the above processing plants is first channelled through a separate network into pre-concentration and only then into the biofilter. Immediately prior to the pneumatic conveyors, an air purifier is in each instance installed, through which all the exhaust air is intensively purified. The purifier is operated with water as the purification agent. The water is supplied in constant circulation. The losses on the basis of evaporation are compensated for through the addition of fresh water. In order to transport away separated fat or solid matter, the purifier can be operated with a constant overflow. The overflow volume must be set in accordance with actual requirements. Ex- perience shows that the effluent volume will be in the region of 0,5 to 1 m3/h. The con- tamination level is comparable with that of plant purification water. In accordance with the results of the dimensioning trials, the biofilter has a surface area of 800 m2. At a planned exhaust air level of 100.000 m3/h, the specific filter surface load will be 125 m3/h. This corresponds with the load of the biofilters that have been in use in comparable plants for many years and have sufficiently proven their effectiveness. The exhaust air is channelled into the chamber under the biofilter and then flows through the filter bed. The filter bed consists of a mixture of fibrous peat and heather. The dwell time of the exhaust air in the filter bed at a planned load of 125 m³/h and a filter bed height in a set state of 0,8 m is approx. 15 to 20 s. During this time, the organic odorants con-
- Seite 233 und 234: Teil 3 Seite 4-6 - Efficient use an
- Seite 235 und 236: Teil 3 Seite 4-8 heat exchangers, p
- Seite 237 und 238: Teil 3 Seite 4-10 The situation wit
- Seite 239 und 240: Teil 3 Seite 4-12 rect evaporation
- Seite 241 und 242: Teil 3 Seite 4-14 Additional heat e
- Seite 243 und 244: Weight loss after 24 hours Temperat
- Seite 245 und 246: 4.2.5 Evisceration Reference to act
- Seite 247 und 248: Achieved environmental benefits Cro
- Seite 249 und 250: 4.5.1 Mechanical treatment 4.5.1.1
- Seite 251 und 252: Teil 3 Seite 4-24 Both in terms of
- Seite 253 und 254: Teil 3 Seite 4-26 4.5.2.1 Ammoniaca
- Seite 255 und 256: Teil 3 Seite 4-28 Brögbern animal
- Seite 257 und 258: Teil 3 Seite 4-30 The decision depe
- Seite 259 und 260: Teil 3 Seite 4-32 closed area can b
- Seite 261 und 262: Teil 3 Seite 4-34 coincides with th
- Seite 263 und 264: Teil 3 Seite 4-36 At a slaughterhou
- Seite 265 und 266: Age of sludge (tTS) Is this of spec
- Seite 267 und 268: Example plants Teil 3 Seite 4-40 Co
- Seite 269 und 270: BSB5 - load Bd (BSB ) NH4 -N - load
- Seite 271 und 272: Fe Fl Fe Fl P D MB Teil 3 Seite 4-4
- Seite 273 und 274: Teil 3 Seite 4-46 Parameters Unit M
- Seite 275 und 276: Teil 3 Seite 4-48 To optimise the m
- Seite 277 und 278: Driving force for implementation Ex
- Seite 279 und 280: Teil 3 Seite 4-52 Table 4-15 Dimens
- Seite 281 und 282: Teil 3 Seite 4-54 liquid fertiliser
- Seite 283: - No cross media effects Teil 3 Sei
- Seite 287 und 288: Decomposition level Measure- Teil 3
- Seite 289 und 290: Teil 3 Seite 6-2 FAT/ HEAT TRANSFER
- Seite 291 und 292: Teil 3 Seite 6-4 Clarification plan
- Seite 293 und 294: Teil 3 Seite 6-6 ENERGY FAT/ HEAT C
- Seite 295 und 296: Teil 3 Seite 6-8 ENERGY/ STEAM INPU
- Seite 297 und 298: Teil 3 Seite 6-10 water if necessar
- Seite 299 und 300: Teil 3 Seite 6-12 - In- vessel comp
- Seite 301 und 302: Teil 3 Seite 6-14 For 1000 kg of de
- Seite 303 und 304: Teil 3 Seite 6-16 Liming is usually
- Seite 305 und 306: Teil 3 Seite 6-18 ceous earth filte
- Seite 307 und 308: See description under 1 Limed bone
- Seite 309 und 310: H Concentration See description und
- Seite 311 und 312: Teil 3 Seite 6-24 The excess acid i
- Seite 313 und 314: Teil 3 Seite 7-1 7 CURRENT CONSUMPT
- Seite 315 und 316: 7.1.1 Rendering 7.1.1.1 Water Teil
- Seite 317 und 318: Teil 3 Seite 7-5 - Cleaning wastewa
- Seite 319 und 320: Teil 3 Seite 7-7 Table 7-5 shows th
- Seite 321 und 322: 7.1.2 Fat melting 7.1.3 Fish meal a
- Seite 323 und 324: Teil 3 Seite 8-1 8 TECHNIQUES TO CO
- Seite 325 und 326: Reference literature Teil 3 Seite 8
- Seite 327 und 328: Teil 3 Seite 8-5 Corporate clarific
- Seite 329 und 330: Economics Driving force for impleme
- Seite 331 und 332: 8.1.9 Rubishes Teil 3 Seite 8-9 8.1
- Seite 333 und 334: Oberding animal carcass disposal pl
Teil 3 Seite 4-58<br />
3. Filtermaterial: exchange each 4 year summation=<br />
14.000 €/a<br />
4. Maintenanance summation=7.000 €/a<br />
5. Cost of operation (summation Nr. 1 - Nr. 4) 93.475 €/a<br />
Driving force for implementation<br />
Example plants<br />
Example plant: Vereinigte Fischmehlwerke Cuxhafen GmbH & Co KG, Germany<br />
At this plant, exhaust air from the sectors:<br />
Boiling apparatuses<br />
Pre-sifting<br />
Presses<br />
Decanters<br />
Dryers<br />
Centrifuges<br />
Concentration plant<br />
is treated.<br />
Since the exhaust air still has a consi<strong>der</strong>able heat content, the intention is to utilise a<br />
portion of this heat during the new pre-concentration. I.e. the exhaust air of the above<br />
processing plants is first channelled through a separate network into pre-concentration<br />
and only then into the biofilter.<br />
Immediately prior to the pneumatic conveyors, an air purifier is in each instance installed,<br />
through which all the exhaust air is intensively purified. The purifier is operated with water<br />
as the purification agent. The water is supplied in constant circulation. The losses on the<br />
basis of evaporation are compensated for through the addition of fresh water. In or<strong>der</strong> to<br />
transport away separated fat or solid matter, the purifier can be operated with a constant<br />
overflow. The overflow volume must be set in accordance with actual requirements. Ex-<br />
perience shows that the effluent volume will be in the region of 0,5 to 1 m3/h. The con-<br />
tamination level is comparable with that of plant purification water.<br />
In accordance with the results of the dimensioning trials, the biofilter has a surface area<br />
of 800 m2. At a planned exhaust air level of 100.000 m3/h, the specific filter surface load<br />
will be 125 m3/h. This corresponds with the load of the biofilters that have been in use in<br />
comparable plants for many years and have sufficiently proven their effectiveness.<br />
The exhaust air is channelled into the chamber un<strong>der</strong> the biofilter and then flows through<br />
the filter bed. The filter bed consists of a mixture of fibrous peat and heather. The dwell<br />
time of the exhaust air in the filter bed at a planned load of 125 m³/h and a filter bed height<br />
in a set state of 0,8 m is approx. 15 to 20 s. During this time, the organic odorants con-