Influence of New WI-BREF on the Concepts of Flue Gas Cleaning in the Future – What Will Change?

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541 Influence of New WI-BREF on the Concepts of Flue Gas Cleaning in the Future – What Will Change?

Flue Gas Treatment

Influence of New WI-BREF on the Concepts of Flue Gas Cleaning in the Future – What Will Change?

Ruediger Margraf

1. IED and WI-BREF ...541

2. Process-related solution approaches ...543

2.1. Particle separation ...543

2.2. Acid crude gases such as HF, HCl and SO_x ...543

2.2.1. Lime-based processes ...543

2.2.2. Dry sorption with NaHCO₃ ...546

2.3. Reduction of NO_x ...546

2.3.1. SNCR-process ...547

2.3.2. Combination of SNCR – Conditioned dry sorption – Wet scrubber ...547

2.3.3. Combined process with the use of SCR ...548

2.4. Heavy metals as well as dioxins/furans ...553

2.4.1. Heavy metals ...553

2.4.2. Dioxins/furans ...554

3. Further major points for discussion concerning WI-BREF ...554

4. Personal assessment ...555

5. References ...556

1. IED and WI-BREF

Following the introduction of Industrial Emission Directive (IED) [4] in 2010, the position of WI-BREF with regard to the approval of new plants and also the continued operation of existing plants changed considerably. With the IED it was stipulated that

• the Best Available Reference Documents (BREF) and by this also the Waste Inci- neration (WI) BREF have to be revised,

• the Best Available Techniques (BAT) Conclusions have to be published in a separate document,

• the BAT Conclusions have to be transferred into national law by the member states of the EU.

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reatment

Table 1: BATAELs (results from Final Meeting TWG)

Results of final meeting Parameter BATAELS (2006) ELV IED(+CI) New BAT-AEL New BAT-AEL

Unit Sampling

for new plants for existing plants period Dust 1 – 5 10 (± 3) < 2 – 5 mg/Nm³ daily

TOC 1 – 10 10 (± 3) < 3 – 10 mg/Nm³ daily

HCl 1 – 8 10 (± 4) < 2 – 6 < 2 – 8 mg/Nm³ daily

HF 1 1 (± 0,4) < 1 < 1 mg/Nm³ daily

SO₂ 1 – 40 50 (± 10) 5 – 30 5 – 40 mg/Nm³ daily

NO_x SCR 40 – 100 200 (± 40) 50 – 120 50 – 150 mg/Nm³ daily

SNCR 120 – 180 50 – 180 mg/Nm³ daily

NH₃ (SNCR) 1 – 10 2 – 10 2 – 10 (15) mg/Nm³ daily

Hg 0.001 – 0.02 50 < 5 – 20 < 5 – 20

µg/Nm³ daily Hg (indicative) over sampling period < 15 – 35 < 15 – 40 indicate half

CO 5 – 30 50 (± 5) < 10 – 50 mg/Nm³ daily

PCCD/F 0,01 – 0,1 0,1 < 0,01 – 0,04 < 0,01 – 0,06 ng/Nm³ PCCD/F + dlPCB < 0,01 – 0,06 < 0,01 – 0,08 ng/Nm³

Cd + Tl 0,005 – 0,05 0,05 0,005 – 0,02 mg/Nm³

Sb+As+Pb+Cr+

Co+Mn+Ni+V 0,005 – 0,5 0,5 0,01 – 0,3 mg/Nm³

hourly

The revision of WI BREF started in 2017. Meanwhile the plant operators have been requested by the European IPPC Bureau to report on the real emission values of the corresponding operational plant. The results will be used for the definition of Best Available Techniques Associated Emission Levels (BATAELs). These BATAELs are forming the basis for the emission limit values in the scope of approval of new plants.

Furthermore, these ranges of values are defining the condition for the continued operation of existing plants. Upon passing of WI BREF, each member state of the EU has to determine statutorily emission limit values within the national framework, taking into account the requirements of BAT Conclusions. With regard to existing plants the proof of new limit values has to be provided within four years.

In 2017 the tentative draft of revised WI-BREF [1] was published. In the meantime, the Final Meeting of Technical Working Group took place in April 2018. As a result the new limit values to be expected have among other things been published (Table 1) [14].

The publishing of BAT Conclusions and final version of WI-BREF is scheduled for the end of 2019. Independent of this, the BATAELs listed in table 1, which are providing the framework for limit values in the future, are of course already influencing the concept selection for the flue gas cleaning of WtE-plants. This lecture discusses possible solution approaches for the reliable observance of BATAELs for the separate pollutants in the gas.

It may be remarked in addition that primarily in the field of thermal incineration the reduction of pollutants such as CO, TOCs etc. has not been taken into consideration.

over sampling period long term sampling

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2. Process-related solution approaches 2.1. Particle separation

In almost all existing flue gas cleaning concepts and also in those of the future, at least one filtering separator is integrated in the form of a bag filter. If a correct design and execution is provided, this type of separator ensures a very efficient and reliable separation of particles of far more than 99.9 % (Figure 1) [13]. As a result of this, the reliable observance of the range shown in Table 1 for future limit values of < 2 up to 5 mg/Nm³ should be possible.

Figure 1: Efficiency of different particle separators

2.2. Acid crude gases such as HF, HCl and SO

_x

2.2.1. Lime-based processes Predominantly lime-based processes have so far been used in new plants for the separation of acid crude gases. Figure 2 shows as an example a design of conditioned dry sorption. Further processes are among other things described in [7].

99.9

Separation curves of different de-dusting systems

η %

99 90

50

10

0

0 0.1 1 10 100

particle size μm

mechanical separator fabric filter

three-bag dry ESP (coal firing) single-bay ESP

wet mechanical separator (scrubber)

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reatment

Figure 2: Schematic view of conditioned dry sorption

These processes allow the reliable compliance with the today requested limit values, with at the same time acceptable operating costs. Figure 3 [10] shows corresponding crude gas and clean gas values for HCl and SO₂ over a period of time of 24 hours.

crude gas

additive additive

AC

filter

clean gas

H₂O

double screw conveyer reactor with conditioning rotor Ca(OH)₂

08:00 16:00 20:00

2,000 1,000 0 -1,000 -2,000 -3,000 -4,000

HCI, SO₂-Crude gas, SO₂-Clean gas mg/Nm³dry

00:00 04:00 12:00

-5,000 4,000 3,000

HCI-Clean gas, Stoichiometry

12 10 8 6 4 2 0 18 16 14

00:00 time

HCI downstream boiler

SO₂ downstream boiler

SO₂ stack HCI stack Stoichiometry

Figure 3: Trend curves for HCl and SO₂ of WtE-plant GML Ludwigshafen

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If particularly for HCl the upper range of BATAELs is requested for the operation of a plant, these requirements can also in the future be achieved with the use of the conditioned dry sorption. As a precaution, additional measures for the coverage of crude gas peaks should be integrated in the process concept.

• Injection of an additive powder, as e.g. NaOH, into an evaporative cooler installed upstream of conditioned dry sorption [15]

• Combination spray absorber and conditioned dry sorption [8]

The efficiency of the combination spray absorber with conditioned dry sorption is shown in Figure 4. The corresponding trend curves for crude gas and clean gas values of HCl and SO₂ of an incineration line of MHKW Rothensee are illustrated over a period of time of 24 hours. At the time of measurement the limit values complied with the requirements of EU Directive 2000/76/EC [5]. The requested limit values will reliably be observed even in case of a stoichiometric factor lower than 1.8. [8]. To allow the observance of more stringent limit values, the stoichiometric factor should be increased slightly.

As far as lower values have to be considered for HCl and SO₂ during design of a new plant, the use of combined processes can be reasonable and/or necessary.

• Combination dry sorption - wet scrubber [11] (see subclause 2.3.2)

• Combination of a dry sorption process using NaHCO₃ with a Ca-based process [9]

2,500 crude gas mg/Nm³ dry

clean gas mg/Nm³ dry

2,000

1,500

1,000

00:00 0:000

10 20 30 40 50

2:00

SO₂ clean gas 4:00 6:00 8:00 10:00 12:00 14:00 16:00 18:00 20:00 22:00 500

HCl crude gas HCl clean gas SO₂ crude gas

Figure 4: Trend curves for HCl and SO₂ of WtE-plant MHKW Rothensee

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2.2.2. Dry sorption with NaHCO₃

The dry sorption with NaHCO₃ competes with process technologies using Ca-based additive powder qualities. The quite simple process technology of the basic variant is shown in Figure 5. Contrary to Ca-based processes, the efficiency will increase with the dry-bulb temperature in the gas when using NaHCO₃. The multiple re-circulation of the particles separated in the filter into the flue gas flow upstream filter is advantageous with regard to the separation efficiency and the stoichiometric factor [12].

filter

ID-fan stack mill

crude gas

NaHCO₃ AC

top filter

In principle, the current typically requested limit values and the upper values of BA- TAELs can be observed with this process, however, compared to Ca-based processes, with higher costs for the provision of additive powders. Due to the reason above, this process has mainly be used for smaller incineration plants. This process may gain in importance in the future in combination with SCR-plants. The advantage in this connection is that NaHCO₃ allows an efficient separation of SO₂ and HCl from acid crude gases, preferably in the case of higher temperatures. A corresponding process variant is discussed under subclause 2.3.3.: Combination of dry sorption with SCR process.

2.3. Reduction of NO

_x

In the draft of WI-BREF, the limit values for NO_x are specified in a very wide range.

• New plants

– NO_x: 50-120 mg/Nm³ – NH₃: 2-10 mg/Nm³

Figure 5:

Basic variant of dry sorption with NaHCO₃

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• Existing plants

– NO_x for SCR 50: 150 mg/Nm³ – NO_x for SNCR 50: 180 mg/Nm³ – NH₃: 2-10 (SNCR 15) mg/Nm³

With regard to existing plants, this offers the opportunity of further operation of sufficiently effective SNCR-systems in the scope of limit values currently valid. Based on the upper values of BATAELs-range, it is still possible to use SNCR-systems for new plants. Regarding the lower range it will surely only be possible to install an SCR-system.

2.3.1. SNCR-process With regard to the investment costs, the SNCR-process constitutes the most cost- effective variant. The achievable emission values with simultaneous observance of requested NH₃-slippage are in the order of 80-100 mg/Nm³. In this connection it must be taken into account that the possibility of a correction of emission value to an O₂-reference content of 11 vol% is not admissible in all countries of EU. As a result of this, a limit value of 80 mg/Nm³ may correspond to a real emission value of 96 mg/Nm³ if the actual O₂-content in the gas totals to 9 vol%.

It has to be expected that in future the use of an SNCR-system alone will no longer be sufficient for a large number of plants. In these cases, either the use of a combined process SNCR with downstream installed scrubber or a process with the use of an SCR-system will become necessary.

2.3.2. Combination of SNCR – Conditioned dry sorption – Wet scrubber This process combination especially represents an alternative when the requested NO_x emission limit values can reliably be kept by means of an SNCR process, however with a higher NH₃ emission. The basic design of this combined process is shown in Figure 6.

boiler

quench

reactor

conditioned dry sorption acid and basic scrubber double shaft

mixer

double shaft mixer, quench SNCR H₂SO₄

NaOH stack AC

Ca(OH)₂ NH₄OH

+ H₂O H₂O

Figure 6: Combination conditioned dry sorption – wet scrubber

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reatment

In this concept, the conditioned dry sorption is operated in such way that the crude gas downstream of this stage only contains low residual concentrations of acid crude gas pollutants. Depending on the application in question, the downstream installed fine cleaning stage serves for the

• separation of NH₃ in an acid scrubber,

• progressing reduction in emission values e.g. for the acid crude gas components,

• heat recovery.

Due to the fact that the acid scrubber only serves as a fine cleaning stage for the reduction of HCl beside the separation of NH₃, the waste water quantity can be kept at a low level. Therefore it will be appropriate to add this waste water above the grate near the incineration.

Figure 7: Emission values exemplary shown at WtE-plant Oulun Energia

To allow an operation free from waste water, the waste water from the basic stage should be added to the system near the conditioned dry sorption.

It may be remarked in addition that when using this combined process, extremely low emission limit values can also be achieved for the acid crude gas pollutants HCl and SO_x (Figure 7).

2.3.3. Combined process with the use of SCR

Combination of conditioned dry sorption with SCR process

As far as NO_x emission limit values as defined at the lower end of the value range between 50 and 120 mg/Nm³ stated in the draft of WI-BREF have to be observed, the

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Messung

Tabelle 1:

Störkomponente Konzentration QE auf die Hg-Messung

SO2 1.000 mg/m2 – 0,065 µg/m3

H2O 30 Vol.-% 0,060 µg/m3

HCI 200 mg/m3 keine QE

NO 300 mg/m3 keine QE

NO2 30 mg/m3 0,090 µg/m3

O2 21 Vol.-% – 0,120 µg/m3

Alle weiteren getesteten QE‘s < ± 0,05 µg/m3

5. Anwendungsbereich des neuen Messverfahrens für die Emissions- und Prozessmessung bei Verbrennungsanlagen Emission

Das neue Messverfahren konnte bereits für die Emissionsüberwachung des Gesamt- anlagen) ohne Leistungseinbußen oder Einschränkungen erfolgreich absolviert.

Für den Standardmessbereich von 0 bis 45 µg/m³ gilt an allen drei Anlagen ein War- tungsintervall von sechs Monaten.

Prozess (Rohgasanwendung)

Aufgrund der einfachen Bauweise und der Gasentnahme ohne zusätzliche Hilfs- und Re- Die Resultate der Testinstallationen zeigen hierbei die Flexibilität des eingesetzten Messver- fahrens, sowohl für den kleinsten Messbereich von 0 bis 10 µg/Nm³, als auch bis in den sehr hohen Konzentrationsbereich von bis zu 4.000 µg/m³ (Bild 10). Eine schnelle, zuverlässige möglich, wieder rot markierte Peak zeigt (Bild 11). Das Messsystem kommt dabei unverän- dert gegenüber der Emissionsmesseinrichtung zum Einsatz und ermöglicht dem Betreiber bzw. unbekannter Zusammensetzung. Im vorliegenden Beispiel an einer kommunalen Hausmüllverbrennungsanlage betrug die Grundlast im Durchschnitt etwa 200 µg/Nm³.

Allerdings traten auch immer wieder Spitzen von bis zu 3.000 bis 4.000 µg/m³ auf, was natürlich entsprechende Maßnahmen für die Gasreinigung, um den Grenzwert von des markierten Peaks verdeutlicht die schnelle Reaktionszeit der Messung sowohl im Anstieg, als auch im Abklingen der Hg-Konzentration (Bild 12).

Sowohl bei Abfallverbrennungsanlagen und insbesondere auch bei Sondermüllver- brennungsanlagen ist das Interesse an diesen Messungen sehr gestiegen. Denn mit der Hg-Rohgasmessung verfügt der Betreiber über eine Überwachung, die zum frühestmög- lichen Zeitpunkt eine mögliche Überladung von Hg für die Abgaswäsche signalisiert und

Messung von Quecksilber

Messung

typischerweise durch SO2 und andere Gaskomponenten bekannt sind, treten bei diesem Verfahren nicht auf (Tabelle 1). Vergleichende Messungen an Anlagen mit bestehenden Quecksilber CEMS zeigen eine hervorragende Übereinstimmung, ebenso im Vergleich zu Optional können für die regelmäßige Qualitätskontrolle der Messungen automatisiert HgCl2-Konzentrationen über eine integrierte Verdampferapparatur aufgegeben werden.

Ejector Messgaszelle 1.000 °C Optik/Detektor Klimagerät Kalibriergas-generator (ohne Abdeckung)

blau= Untergrundmessung;

orange= Hg-Absorptionsmessung Hg-Linienaufspaltung durch Magnetfeld an der Lichtquelle Bild 7: Schrankansicht des kontinuierlichen Quecksilber-Messverfahrens MERCEM300Z (außen und innen)

Bild 9:

Quarzmessgaszelle bei 1.000 °C zur Konvertierung und gleich- zeitigen Echtzeitmessung (pa-

Immissionsschutz, Volume 1 Released: 2010

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ISBN: 978-3-935317-90-0 Hardcover: 664 pages Price: 40.00 EUR Immissionsschutz, Volume 4

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Package Price

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save 80.00 EUR Immissionsschutz, Volume 5

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installation of an SCR-process will in any case become necessary. In this connection the preferred temperature range for the catalyst lies in a range of 220 °C up to 240 °C. This temperature range allows a sufficiently good transformation speed.

Problems due to the formation of ammonium sulphate can reliably be exclu- ded, as far as the temperature-dependent SO₂ content in the gas is lower than 10-25 mg/Nm³. Due to the preferred temperature range for the conditioned dry sorption of approximately 130 °C up to 150 °C, a reheating of gases upstream of the catalyst is unavoidable. The reheating of gases can indeed largely be realised by heat recycling around the catalyst, however, the remaining temperature difference of approximately 30 K has to be balanced by an external heat input, e.g. by means of a steam-gas-heat exchanger. A downstream installed heat exchanger located upstream of stack can be used for the heat recovery, but the generated heat has a comparatively poor quality. Figure 8 shows the basic scheme of a corresponding process.

Figure 8: Combination conditioned dry sorption – SCR

If very low limit values are also requested for further pollutants such as acid crude gas pollutants, heavy metals, dioxins/furans, an additional dry sorption stage can be installed downstream of SCR-system. A correspondingly designed and installed plant including the achieved annual average values are shown in Figure 9. Details concerning this plant concept can be gathered from the references [9].

H₂O H₂O

reactor

compressed air ammonia

water tank

condensate saturated steam

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reatment

Figure 9: Emission values of WtE-plant Enertec Hameln, line 4

Combination of dry sorption with SCR process

Due to the fact that the separation of acid crude gas pollutants, and in this respect particularly SO_x, is very efficiently possible by injection of NaHCO₃ in a temperature range of 220 °C up to 240 °C, the reheating can be omitted in case of a combination of dry sorption with NaHCO₃ and a downstream installed catalyst. Figure 10 shows a possible process variant.

The separation of acid crude gas pollutants takes place in the first dry sorption stage at a temperature of approximately 240 °C by means of injection of NaHCO₃. Following this, the ammonia water injection, the mixing section and the catalyst are arranged.

In an external economiser installed downstream of catalyst, the gas is cooled down to approx. 140-120 °C. Another dry sorption stage serves for the reliable separation of the acid pollutants still existing in the gas, the heavy metals including mercury as well as dioxins/furans by means of injection of Ca(OH)₂ and activated carbon. This arrangement does not only allow the achievement of low NO_x and NH₃ values, but also ensures a very good separation efficiency for acid crude gases with at the same time low additive powder consumption. However, when evaluating the economic efficiency, the high specific purchase price for NaHCO₃ has to be compared to the cost savings resulting from the omission of steam-gas-heat exchanger.

The use of a low temperature catalyst can be an alternative to the above-described process. Due to the operation of SCR at approximately 180 °C up to 200° C, activated carbon can be injected in the dry sorption stage. However, this variant presents the high risk of efficiency loss of catalyst stage due to the formation of ammonium salts.

A cyclic regeneration of catalyst by means of gas heating will be necessary.

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Figure 10: Process variant for the combination dry sorption with SCR

2.4. Heavy metals as well as dioxins/furans

2.4.1. Heavy metals Where heavy metals (except for Hg and Hg-compounds) are present in gaseous form due to their steam pressure, they can be converted into particulate compounds by means of chemical reactions with the basic additive powder qualities. In case of a sufficient quantity of basic additive powder qualities, a separation reliably takes place even in case of temperatures higher than 200 °C. Measuring results clearly show that emission limit values to be expected in the future for heavy metals can reliably be achieved by means of injection of Ca- or Na-based additive powder qualities in combination with a particle filter.

The separation of Hg and Hg-compounds will in most of the cases be achieved by ad- sorption at additive powders with large specific surface. Usually, activated coke and/

or activated carbon are used for this purpose. Normally the limit value totalling to 10 µg/Nm³ which is already currently requested as annual average value in Germany, can be achieved with this process.

The continuous measurement of Hg limit values already generally required in Ger- many and expected for all other EU countries in the future, has led to the fact that many plants have meanwhile been equipped with precautionary measures for the separation of Hg peaks. In this connection especially the additional injection of do- ped activated carbon in case of increasing emission limit values may be mentioned.

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reatment

The injection of additional liquid additive agents into an evaporative cooler installed upstream of the conditioned dry sorption system may present a further measure [6].

Even acid scrubbing stages installed downstream of a condition dry sorption system may contribute to the Hg separation.

2.4.2. Dioxins/furans

The emission limit value for dioxins/furans will intensify significantly as a result of revision of WI-BREF (Table 1). There is a large number of measuring results available for the injection of carbonaceous additive powder qualities with large specific surface areas in connection with a bag filter, partly clearly below the range of BATAELs according to Table 1. Nevertheless, individual measurements are also known, showing emission values lower than 0.1 ng/Nm³ which are, however, lying above the upper limit of the reworded BATAELs. In this context a precise operating mode of plant has to be ensured in future in order to avoid an exceeding of emission limit values.

• Low CO-values

• Low particle contents in the clean gas downstream filter

• Adequate injection quantities of carbonaceous additive powder qualities Multi-stage flue gas cleaning systems are surely an advantage in this respect.

It should also be noted that in the scope of revision of WI-BREF the use of continuous sample taking for the constant monitoring of dioxin/furan emissions is being debated.

In this connection experiences are among others available in Belgium.

3. Further major points for discussion concerning WI-BREF

Apart from the emission limit values there are further items which are discussed in the scope of the revision of WI-BREF. The following two major points are discussed in connection with the BATAELs:

Normal operating conditions (NOCs) und others than normal operating conditions (OTNOCs)

According to IED [4], the emission limit values are referring to the normal operating conditions. However, the IED is making an exception with regard to waste incinerators and refers in this context to the effective operating time as basis for the observance of emission limit values. The effective operating time comprises a larger operational range and can also include others than normal operating conditions. Due to the fact that the draft does not provide a clear allocation, there might be a need for discussions in the future concerning the granting of approvals.

The above-mentioned continuous sample taking in connection with dioxins/furans is an example for this. The question arises, when the measurement has to be connected, e.g. during cold start-up of a incineration line, and which further operating conditions will be evaluated as OTNOCs. The discussion has not been finalised in this respect.

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Measuring uncertainty Particularly the lower end of BATAEls range is subject to the risk that measuring tole- rances, as requested in the IED, cannot be achieved, thus presenting a high measuring uncertainty for these values (Figure 11).

Figure 11: Measurements uncertainties

It is important to make sure that the new WI-BREF will comprise a definitive clarifi- cation. Based on the current state of discussion, the WI-BREF will contain a reference concerning the observance of the measuring uncertainty. The question, however, remains open, whether this reference will also be included in chapter 5 (BAT Conclusions).

Nevertheless this will absolutely be necessary as only this part has to be transferred into national law. [3]

4. Personal assessment

The whole range of BATAELs to be expected in the scope of revision of WI-BREF can reliably be achieved with the available process-related solutions for the flue gas cleaning in the field of waste-to-energy. However, in many cases multi-stage and - in comparison to today’s plants - more complex systems will have to be used. The disadvantage of higher investment costs frequently associated with this, will in many cases be at least partially be compensated by lower operating costs.

It remains to be seen which limit values will each be stipulated in national law as binding values by the separate member states of the EU. Even if, however, the upper end of BATAELs ranges will be taken as basis in this context, the lower values will in all probability be discussed in the scope of public participation during approval pro- cedures for new plants.

From the author’s point of view it will definitely be necessary that not only the BATAELs but also further items will be defined precisely in the final version of WI-BREF and particularly in the BAT Conclusions. This refers among other things to the discussion about measuring uncertainty and to NOC and/or OTNOC.

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reatment

Finally, it has to be noted that there are still considerable differences among the member states of the EU concerning the handling of thermally recyclable residues (Figure 12 [2]).

Even if the statistic is based on an investigation in 2015 and although changes have been realised in the meantime in some countries, as e.g. Great Britain and Finland, regarding the reduction of landfilling, the statistic is still correct generally. There is still a large number of countries in which thermally reusable residues, which can no longer be recycled, are partly or completely deposited. With regard to the effects on the environment, the installation of waste-to-energy plants with limit values at the upper end of BATAELs will in this connection surely be better than the further landfilling of these materials, on the grounds that thermal recycling plants are not financially feasible.

Figure 12: Shares of recycling, WTE and landfill in Europe

5. References

[1] Best Available Techniques (BAT) Reference Document on Waste Incineration, Draft 1 (May 2017)

[2] CEWEP: http://www.cewep.eu/wp-content/uploads/2017/08/Graph-3-treatments.pdf [3] Clerens, P.; Walczak, N.: Impact of EU Legislative Developments on the Waste-to-Energy Sec-

tor. In: Thomé-Kozmiensky, K. J.; Thiel, S.; Thomé-Kozmiensky, E.; Winter, F.; Juchelková, D.

(Eds.): Waste Management, Volume 7, Waste-to-Energy. Neuruppin: TK Verlag Karl Thomé- Kozmiensky, 2017, pp. 3-13

[4] European Parliament, European Council: Directive 2010/75/EU of 24 November 2010 on industrial emissions (integrated pollution prevention and control), 2010

Municipal waste treatment in 2016 EU 28 + Switzerland, Norway and Iceland

landfill 25

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4 57 27

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Netherlands

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Spain Portugal*

Estonia Slovenia LithuaniaPolandIreland** Slovakia CyprusRomaniaGreece Czech Republic

Malta Hungary Bulgaria LatviaCroatia

SwitzerlandNorw ay

Iceland Waste-to-Energy recycling and composting

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[5] European Parliament, European Council: Directive 2000/76/EC of 4 December 2000 on the incineration of waste, Official Journal of the European Communities, 28.12.2000

[6] Fritsche, J.: Aktivkohle AddSorb VQN u. EcoSorb QS Advanata in der Rauchgasreinigung, VDI- Wissensforum Betriebsmittel in der Rauchgasreinigung, Mannheim 2014

[7] Löschau, M.; Kersting, M.: Energieeffizienz bei der Abgasreinigung. In: Thomé-Kozmiensky, K. J.; Beckmann, M. (Eds.): Energie aus Abfall, Band 7. Neuruppin: TK Verlag Karl Thomé- Kozmiensky, 2010, pp. 619-637

[8] Lücker, G.: Optimierung der Sprühabsorption des MHKW Rothensee – Eine Herausforderung?

In: Thomé-Kozmiensky, K. J.; Beckmann, M. (Eds.): Energie aus Abfall, Band 12. Neuruppin:

TK Verlag Karl Thomé-Kozmiensky, 2015, pp. 327-346

[9] Margraf, R.: Dry, Semi-dry or Wet – Which System Fits Best Depending on the Overall Condi- tions? – In: Thomé-Kozmiensky, K. J.; Thiel, S.; Thomé-Kozmiensky, E.; Winter, F.; Juchelková, D. (Eds.): Waste Management, Volume 7, Waste-to-Energy. Neuruppin: TK Verlag Karl Thomé- Kozmiensky, 2017, pp. 431-447

[10] Margraf, R.: Simple and Effective – the Conditioned Dry Sorption Process for Flue Gas Treat- ment Downstream Waste Incinerators. In: Thomé-Kozmiensky, K. J. (Eds.): Waste Management, Volume 5. Neuruppin: TK Verlag Karl Thomé-Kozmiensky, 2015, pp. 253-267

[11] Margraf, R.: TwinSorp® – a simple process for increased requirements on the emission limit values i. a. for waste and RDF incinerators, considering the energy efficiencycommand, 6th symposium; Dry crude gas cleaning for solid fuel firings and thermal process technology, Haus der Technik Essen, 2010

[12] Margraf, R.: Trockensorption mit Natriumbicarbonat – wirklich ein ganz einfaches Verfahren?, Examinations at a waste incinerator in France; 5th symposium, Dry crude gas cleaning for solid fuel firings and thermal process technology, Haus der Technik Essen, 2009

[13] Schulteß, W.: Presentation material Ing.-Büro Prof. Schulteß

[14] Technical Working Group (tWG) Draft conclusions of the Final Meeting or the review of the BAT reference document on Waste Incineration (WI BREF), European IPPC Bureau, Seville, 23.–27. April 2018

[15] Wradatsch, R.: Entwicklung und Betriebserfahrungen mit der konditionierten Trockensorp- tion des MHKW Ludwigshafen, 3. Fachtagung Trockene Abgasreinigung für Festbrennstoff- Feuerung und thermische Prozesstechnik, Haus der Technik Essen, 2007

Contact Person

Ruediger Margraf, Graduated engineer LUEHR FILTER GmbH

Managing director Enzer Straße 26 31655 Stadthagen GERMANY

Phone: 0049 - 57 21 - 7 08 - 2 00 Email: r.margraf@luehr-filter.com

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Dorfstraße 51

D-16816 Nietwerder-Neuruppin

Phone: +49.3391-45.45-0 • Fax +49.3391-45.45-10 E-Mail: order@vivis.de

TK Verlag GmbH

order now www. .de

Elisabeth Thomé-Kozmiensky

1.5. Generalunternehmer (Planung und Ausführung) Deutsche Babcock Anlagen GmbH

Kesselerneuerung Von Roll Inova, resp. HITACHI Zosen Inova Turbinenerneuerung

1.6. Genehmigungsbehörde Regierung von Oberfranken Ludwigstraße 20 95444 Bayreuth

1.7. Aufsichtsführende Behörde Bayerisches Landesamt für Umweltschutz Bürgermeister Ullrich-Straße 160 86179 Augsburg 1.8. Inbetriebnahme

1978: Linien 1 + 2 und

Klärschlammbehandlung

1981: Linie 3

1982: Erweiterung um Stromerzeugung 1982-1988: Fernwärmeauskopplung und -verteilung 1990: Feuerraumoptimierung, 1. Erweiterung der Abgasreinigungsanlage 1996: Abgasreinigungsanlage2. Erweiterung der

Bild 3:

Abwasserbehandlung und Schlammentwässerung

Löschwasserbecken Notstrom- aggregate 3+4 Katalysatoren

(SCR)

Gewebefilter Öl- tank

Waage Zentral-lager Grundstücksgrenze

Ausdehnungs- gefäß

Energieteil Abwärmenutzung Heizwerk 1 Abfall- bunker lieferungAn- Klärschlamm- Stapelbehälter

Kessel-hausElektro-filter

Teich Luftkondensator Maschinenhaus für neue Turbine/Generator Wertstoffhof

Stadt Bamberg

Kompostieranlage Kläranlagengelände

AVA Augsburg

3. Abfallaufkommen Abfallarten

Hausmüll: 131.103 t

hausmüllähnlicher Gewerbemüll: 81.835 t

Sperrmüll: 14.204 t

Krankenhausabfälle: 3.363 t

insgesamt: 230.505 t

4. Kapazität, Durchsatz und Geometrie Kapazität (Auslegung) 255.000 t/a davon

• Siedlungsabfälle: 251.500 t/a

• Krankenhausabfälle: 3.500 t/a bei einem Heizwert von 9,2 MJ/kg Durchsatz (Siedlungsabfälle)

Durchsatz 2014: 238.224 t

Durchsatz (Krankenhausabfälle)

Abmessungen des Baukörpers 235.000 m2

Bauhöhe ohne Kamin: 38 m

5. Anlieferung und Lagerung Abfallanlieferungen mit: LKW

~ 35.000 Anlieferungen/Jahr 5.1. Waage Hersteller:

Bauart: Brückenwaage

Anzahl: 3

5.2. Anlieferungshalle/Entladestation Anzahl der Abkippstellen: 12 5.3. Bunker für feste Abfälle Abfallart: Siedlungsabfälle Maße (l x b x h) 55 m x 13 m x 25 m nutzbares Volumen: 10.000 m3

Nutzmasse: ~ 5.000 t

Anzahl der Abkippstellen: 12 Abfallart: Krankenhausabfälle nutzbares Volumen: 5.000 m3 5.4. Bunker für Schlacken nutzbares Volumen: ~ 500 m3

5.5. Betriebsmittellagerung

Heizöl: ~ 80 m3

Ammoniakwasser: ~ 60 m3

Kalksilo: ~ 50 m3

Natronlauge: ~ 50 m3

Bild 4: Müllfahrzeuge beim Abkippen von Abfall in Müllbunker Bild 5: Schlackehalle der AVA Augsburg

Waste-to-Energy Plants

– Germany –

The actual book 2016|2017 carries forward the survey of waste-to-energy plants in the Federal Republic of Germany which started in the 1990´s. With the first publication we have two books which complement each other perfectly. Both books provide extensive information about the installed technology and the environmental impact of the waste-to-energy plants. The quality of the new inquiry has been extended in terms of the technical data. Existing gaps regarding the data were partially filled.

This is the result from the considerable assistance of numerous plant operators. The publication on hand shall be seen as an interims report. The work on the data acquisition will be continued. For this reason we ask plant operators and manufactures to critically review the release data.

• 33 minucipal solid waste incineration plant

• 7 solid recovered fuel power plant

• 1 Sonderabfallverbrennungsanlage

The further investigations will be extended to the missing German waste-to-energy plants as well as to plants in other countries.

2014 | 2015

ISBN: 978-3-944310-26-8 Hardcover: 581 Pages,

with coloured illustrations Price: 45.00 EUR

2016 | 2017

ISBN: 978-3-944310-38-1 Hardcover: 407 Pages,

with coloured illustrations Price: 68.00 EUR

ABFALLVERBRENNUNGSANLAGEN – Deutschland –

2014 | 2015 Elisabeth Thomé-Kozmiensky

Editor: Elisabeth Thomé-Kozmiensky

ABFALLVERBRENNUNGSANLAGEN – Deutschland –

2016 | 2017 Elisabeth Thomé-Kozmiensky – Deutschland –

– Deutschland – – Deutschland –

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Vorwort

4

Bibliografische Information der Deutschen Nationalbibliothek Die Deutsche Nationalbibliothek verzeichnet diese Publikation in der Deutschen Nationalbibliografie; detaillierte bibliografische Daten sind im Internet über http://dnb.dnb.de abrufbar

Thiel, S.; Thomé-Kozmiensky, E.; Winter, F.; Juchelková, D. (Eds.):

Waste Management, Volume 8 – Waste-to-Energy –

ISBN 978-3-944310-42-8 Thomé-Kozmiensky Verlag GmbH

Publisher: Thomé-Kozmiensky Verlag GmbH • Neuruppin 2018 Editorial office: Dr.-Ing. Stephanie Thiel, Dr.-Ing. Olaf Holm,

Elisabeth Thomé-Kozmiensky, M.Sc.

Layout: Janin Burbott-Seidel, Ginette Teske, Roland Richter, Cordula Müller, Sarah Pietsch, Gabi Spiegel, Lena Bischkopf

Printing: Universal Medien GmbH, Munich

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