BE1025690B1 - Method and system for the incineration of waste comprising nitrogen-bound components - Google Patents

Abstract

A method of incinerating waste comprising nitrogen-bound components, the method comprising the steps of: providing a first stream of waste and a second stream of waste; introducing the first stream of waste into a burner zone; oxidizing the first stream of waste at a first temperature range in the burner zone to form NO x; introducing oxidised waste containing NOx and the second stream of waste into a combustion zone; and mixing the NOx-containing oxidized waste and the second stream of waste in the combustion zone at a second temperature range such that NOx concentration in the combustion zone is lowered.

Description

EUROPEM TECHNOLOGIES NV, Duwijckstraat 17, 2500 LIER Belgium;

represented by

D'HALLEWEYN Nele Veerle Trees Gertrudis, Meir 24 bus 17, 2000, ANTWERP;

a Belgian invention patent with a duration of 20 years granted, subject to payment of the annual fees as referred to in Article XI.48, § 1 of the Economic Law Code, for: Method and system for the incineration of waste containing nitrogen-bound components.

INVENTOR (S):

GOEMANS Marcel Gerardus Edmond, Kortrijksestraat 361, 3010, KESSEL-LO;

LIKSZA Wojciech Krzysztof, Patrijsweg 9, 2500, LIER;

PRIORITY :

DIVISION:

Split from basic application:

Submission date of the basic application:

Article 2. - This patent is granted without prior research into the patentability of the invention, without guarantee of the merit of the invention or of the accuracy of its description and at the risk of the applicant (s).

Brussels, 11/06/2019,

With special authorization:

BE2017 / 5802

Method and system for the incineration of waste comprising nitrogen-bound components

FIELD OF THE INVENTION

The field of the invention relates to a method and system for the incineration of waste comprising nitrogen-bound components.

BACKGROUND

Prior art solutions for the incineration of waste comprising nitrogen-bound components such as ammonia typically relate to the incineration of waste in a burner placed in a combustion chamber. High amounts of potentially contaminating nitrogen oxides (NOx) are formed during this process. To reduce or eliminate the NOx formed, prior art solutions use either selective non-catalytic reduction (SNCR) or selective catalytic reduction (SCR). In the case of SNCR, the NOx levels formed are reduced by injecting ammonia or urea into the flue gases in the combustion chamber, the flue gases having a temperature of about 900 to 1100 ° C. In the case of SCR, the NOx levels formed are reduced by injecting, in addition to possible ammonia or urea, a catalyst into the flue gases, the flue gases having a temperature of about 200 to 450 ° C.

These prior art solutions are considered to be traditional end-of-pipe solutions that require the consumption of a reagent such as ammonia or urea, the use of additional equipment for injecting the reagent, and high power consumption.

SUMMARY OF THE INVENTION

The purpose of embodiments of the invention is to improve the incineration of waste containing nitrogen-bound components such that lower levels of NOx are achieved in a more efficient manner. More specifically, it is an object of embodiments of the invention to achieve higher energy efficiency by reducing reagent and / or catalyst injection.

According to a first aspect, a method is provided for the incineration of waste comprising nitrogen-bound components, the method comprising the steps of:

- providing a first stream of waste and a second stream of waste;

- introducing the first stream of waste into a burner zone;

BE2017 / 5802 · oxidizing the first stream of waste at a first temperature range in the burner zone to form NOx;

· Entering the NOx-containing oxidised waste and the second stream of waste into a combustion zone; and

- mixing the NOx-containing oxidized waste and the second stream of waste in the incineration zone at a second temperature range such that NOx concentration in the incineration zone is lowered. It is apparent to those skilled in the art that to generate NOx by oxidizing the first stream of waste, this first stream of waste comprises nitrogen-bound components such that the first stream of waste has a potential to form NOx. The second waste stream preferably comprises nitrogen-bound components such that the second waste stream contains ammonia and / or has potential to form ammonia.

Embodiments of the method according to the invention are based, inter alia, on the inventive insight that by providing two waste streams, a first stream of non-potential to form NOx initially burned at a first temperature range, and a second waste stream comprising ammonia and / or has potential to form ammonia that is added only after the first waste stream has been initially burned and oxidized, the second waste stream being used to reduce and / or eliminate NOx formed by burning the first waste stream. In other words, according to embodiments of the invention, waste streams, in particular nitrogen-bound components in the waste streams, are used to promote a deNOx reaction. Ammonia (NH3) present in the second waste stream will react with the previously formed NOx in the oxidized first waste stream at a second temperature range to form nitrogen gas (N2) and water (H2O). In this way less energy is used in comparison with prior art solutions since no or fewer deNOx agents are used and since fuel consumption, and thereby the emission of carbon dioxide, is reduced.

In a preferred embodiment, the method comprises the steps of:

- introducing the mixture of oxidized waste and the second stream of waste into a conditioning zone; and

- cooling the mixture of oxidized waste and the second stream of waste in the conditioning zone at a third temperature range.

In this way, flue gases from the mixture of oxidized waste and the second waste stream can be prepared for ejection in an efficient manner. In a preferred embodiment, cooling is carried out by means of an injection of cooling air.

BE2017 / 5802

The cooling air can, for example, be supplied by means of electro-pneumatic air dampers. In an alternative embodiment, cooling is carried out by extracting heat by means of heat-exchanging surfaces in the conditioning zone, for example by boiler coil (s) and / or membrane wall (s). In yet another alternative embodiment, cooling is carried out by means of injection of water, or low calorific effluents or any cooling gas.

In a preferred embodiment, the method comprises the steps of:

- introducing the mixture of oxidized waste and the second waste stream into a catalyst zone; and

- introducing a catalyst into the catalyst zone at a fourth temperature range such that NO x concentration in the catalyst zone is lowered.

Respond in this way! residual NOx in the flue gases of the mixture, if there is any remaining NOx, with the catalyst, for example ammonia, to form nitrogen gas and water.

In a preferred embodiment, the first temperature range is between 850 and 2000 ° C, preferably between 1000 and 1500 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C.

In this way, the oxidation reaction of nitrogen-bound components, such as ammonia, is the most efficient. In addition, this first temperature range allows fragrant components in the waste to be substantially completely eliminated or destroyed.

In a preferred embodiment, the second temperature range is between 800 and 1000 ° C, preferably "between 850 and 950 ° C, more preferably" between 875 and 940 ° C, and most preferably between 900 and 935 ° C.

In this way a suitable environment is provided to promote a stable and effective reaction of nitrogen oxide and / or nitrogen dioxide with ammonia to water and nitrogen gas.

In a preferred embodiment, the third temperature range is between 350 and 950 ° C, preferably between 400 and 935 ° C, more preferably between 450 and 850 ° C.

In a preferred embodiment, the fourth temperature range is between 150 and 650 ° C, preferably between 200 and 500 ° C, more preferably between 230 and 450 ° C, and most preferably between 320 and 380 ° C.

BE2017 / 5802

In a preferred embodiment, introducing the first stream of waste into the burner zone includes checking the amount of waste in the first stream based on a concentration of nitrogen-bound components in the second stream of waste. Preferably, nitrogen-bound components are monitored in-line for the first stream of waste, while ammonia and / or urea are monitored in-line for the second stream of waste.

In this way it is possible, by controlling the amount of waste, in particular the amount of nitrogen-bound components, in the first waste stream, by means of a forward link, to check the amount of NOx formed by burning the first waste stream on based on the available ammonia and / or urea present in the second waste stream, such that the ratio of NOx to nitrogen-bound components in the combustion zone is optimally suited for reacting to nitrogen gas and water. Preferably the amount of waste in the first waste stream is controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.5. More preferably, the amount of waste in the first waste stream is controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.1.

In a preferred embodiment, introducing the first stream of waste into the burner zone comprises controlling the amount of waste in the first stream on the basis of a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone.

In this way, by checking the amount of waste, more specifically the amount of nitrogen-bound components, in the first waste stream, by means of a feedback, it is possible to check the amount of NOx formed by burning the first waste stream on basic NOx measurements, such that the ratio of NOx to nitrogen-bound components in the combustion zone is optimally suited for reacting to nitrogen gas and water. Preferably the amount of waste in the first waste stream is controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.5. More preferably, the amount of waste in the first waste stream is controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.1.

In a preferred embodiment, a concentration of NOx and / or urea and / or ammonia is measured at the end of the combustion process. Based on these measurement (s), the amount of nitrogen-bound components in the first waste stream and / or the amount of urea and / or ammonia in the second waste stream can be checked.

BE2017 / 5802

A concentration of NOx can be enjoyed by extracting a quantity of flue gas from the relevant zone and analyzing the extracted quantity to calculate the quantity of NOx. When calculating the amount of NOx, a flow rate during extraction can be taken into account. The amount of gas extracted can be processed before an actual analysis is carried out. The amount of gas extracted can, for example, be cooled and / or dried before it is sent to an analyzer to calculate the NOx concentration. A similar extraction can be carried out for measuring a concentration of urea and / or ammonia and / or other nitrogen-bound components.

Checking the amount of waste in the first stream can include: monitoring the composition of the first waste stream, and more particularly the concentration of nitrogen-bound components, and checking the steam cleanliness of the first stream based on NOx levels in the burner zone, combustion zone, conditioning zone and / or catalyst zone.

In a preferred embodiment, introducing the second stream of waste into the combustion zone comprises controlling the amount of waste in the second stream based on a concentration of nitrogen-bound components in the first stream of waste. Preferably, nitrogen-bound components are monitored in-line for the first stream of waste, while ammonia and / or urea are monitored in-line for the second stream of waste.

In this way it is possible, by controlling the amount of waste, in particular the amount of nitrogen-bound components, in the second waste stream, to check by means of a forward link the amount of nitrogen-bound components that will be available to react with NOx that is formed by burning the first waste stream, such that the ratio of NOx to nitrogen-bound components in the combustion zone is optimally suited for reacting to nitrogen gas and water. The amount of waste in the second waste stream is preferably controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.5. More preferably, the amount of waste in the second waste stream is controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.1. In a preferred embodiment, introducing the second stream of waste into the combustion zone comprises controlling the amount of waste in the second stream based on a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone.

In this way it is possible, by controlling the amount of waste, in particular the amount of nitrogen-bound components, in the second waste stream, by means of a

BE2017 / 5802 feedback, control the amount of nitrogen-bound components that will be available to react with NOx that is formed by burning the first waste stream in the burner zone and that reaches the combustion zone, such that the ratio of NOx to nitrogen-bound components in the combustion zone is optimally suited for reacting to nitrogen gas and water. The amount of waste in the second waste stream is preferably controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.5. More preferably, the amount of waste in the second waste stream is controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone is between 1.0 and 1.1.

A concentration of NOx can be measured by withdrawing an amount of flue gas from the relevant zone and analyzing the extracted amount to calculate the amount of NOx. When calculating the amount of NOx, a flow rate during extraction can be taken into account. The amount of gas extracted can be processed before an actual analysis is carried out. The amount of gas withdrawn can, for example, be cooled and / or dried before it is sent to an analyzer to calculate the NOx concentration. A similar extraction can be carried out for measuring a concentration of urea and / or ammonia and / or other nitrogen-bound components.

Checking the amount of waste in the second stream can include monitoring the composition of the second waste stream, and more particularly the concentration of nitrogen-bound components, and controlling the steam rate of the second stream based on NOx levels in the burner zone, combustion zone, conditioning zone and / or catalyst zone.

In a preferred embodiment, introducing the NOx-containing oxidized waste into the combustion zone comprises forwarding the NOx-containing oxidized waste from the burner zone through at least one mixing wall in the direction of the combustion zone.

In a preferred embodiment, the method comprises the step of introducing an additional amount of nitrogen-bound components into the combustion zone.

In this way, when not all NOx has reacted with nitrogen-bound components in the second waste stream, the surplus NOx can react with the additionally introduced nitrogen-bound components such as ammonia and / or urea. Preferably, an additional amount of nitrogen-bound components is determined such that a stoichiometric ratio of NOx to nitrogen-bound components, e.g., ammonia and / or urea, in the combustion zone is between 1.0 and 1.5. More preferably, the additional amount of

BE2017 / 5802 nitrogen-bound components determined in such a way that a stoichiometric ratio of NOx to nitrogen-bound components, eg ammonia and / or urea, in the combustion zone is between 1.0 and 1.1.

In a preferred embodiment, a concentration of NOx and / or urea and / or ammonia is measured at the end of the combustion process. Based on these measurement (s), the amount of nitrogen-bound components in the first waste stream and / or the amount of urea and / or ammonia in the second waste stream and / or the additional amount of urea / ammonia that must be introduced into the incineration zone. checked.

In a preferred embodiment, the method further comprises the step of checking the first temperature range in the burner zone based on at least one of:

- a concentration of NOx in the burner zone;

- a concentration of NOx in the combustion zone;

- a concentration of NOx in the conditioning zone;

- a concentration of NOx in the catalyst zone;

- a concentration of nitrogen-bound components in the first stream of waste; and

- a concentration of nitrogen-bound components in the second stream of waste.

The first temperature range can be controlled by checking an amount of oxygen and / or combustion air in the burner zone. More in particular, an amount of excess air can serve as cooling air in the burner zone. By controlling this amount of excess air, in an exemplary embodiment, the first temperature range can be controlled such that a stoichiometric ratio of NOx to nitrogen-bound components, e.g., ammonia and / or urea, in the combustion zone between 1.0 and 1.5, and preferably between 1.0 and 1.1 is. In addition to controlling the temperature, the concentration of nitrogen-bound components in the first and / or second stream of waste can be controlled based on a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone. In other words, different parameters can be adjusted individually or in combination by monitoring a concentration of NOx during at least one step of the combustion process to achieve an improved reduction of NOx during the combustion process. Examples of such parameters without limitation are; a concentration of nitrogen-bound components in the first and / or second stream of waste, and added stream of urea and / or ammonia, a temperature in any of the burner zone, incineration zone, conditioning zone, and catalyst zone. In a preferred embodiment, the parameters described above are adjusted on the basis of a concentration of NOx and / or urea and / or ammonia measured at the end of the combustion process.

BE2017 / 5802

In an alternative embodiment, the first temperature can be controlled by means of heat exchange surfaces in the burner zone such as one or more boiler coil (s) and / or membrane wall (s). In yet another embodiment, temperature control is achieved by injecting water, low calorific waste streams or any cooling gas.

In a preferred embodiment, the method further comprises the step of checking the second temperature range in the combustion zone based on at least one of:

- a concentration of NOx in the burner zone;

- a concentration of NOx in the combustion zone;

- a concentration of NOx in the conditioning zone;

- a concentration of NOx in the catalyst zone;

- a concentration of nitrogen-bound components in the first stream of waste; and

- a concentration of nitrogen-bound components in the second stream of waste.

The second temperature range can be controlled by controlling an amount of oxygen and / or combustion air in the burner zone. More in particular, an amount of excess air can serve as cooling air in the burner zone. By controlling this amount of excess air, in an exemplary embodiment, the second temperature range can be controlled such that a stoichiometric ratio of NOx to nitrogen-bound components, for example ammonia and / or urea, in the combustion zone between 1.0 and 1.5, and preferably between 1.0 and 1.5 Is 1.1. In addition to controlling the temperature, the concentration of nitrogen-bound components in the first and / or second stream of waste can be controlled based on a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone. In other words, different parameters can be adjusted individually or in combination by monitoring a concentration of NOx during at least one step of the combustion process to achieve an improved reduction of NOx during the combustion process. Examples of such parameters without limitation are; a concentration of nitrogen-bound components in the first and / or second stream of waste, and added stream of urea and / or ammonia, a temperature in any of the burner zone, incineration zone, conditioning zone, and catalyst zone. In a preferred embodiment, the parameters described above are adjusted on the basis of a concentration of NOx and / or urea and / or ammonia measured at the end of the combustion process.

In an alternative embodiment, the second temperature can be controlled by means of heat exchange surfaces in the burner zone such as one or more boiler coils and / or membrane wall (s). In yet another embodiment, temperature control is achieved by injecting water, low calorific waste streams or any cooling gas.

BE2017 / 5802

In a preferred embodiment, the nitrogen-bound components comprise any of ammonia, urea, and nitrogen gas. In a preferred embodiment, the waste comprising nitrogen-bound components is any of the following: a waste gas, a waste liquid, waste sludge, solid waste, or any combination thereof. In an exemplary embodiment, the first stream of waste originates from the same waste source as the second stream of waste, whereby the first stream of waste has a similar composition compared to the second stream of waste. In another embodiment, the first stream of waste is from a different waste source as the second stream of waste, whereby the first stream of waste has a composition different from the composition of the second stream of waste. In an exemplary embodiment, the first stream of waste comprises nitrogen-bound components that contain solid waste and the second stream of waste comprises a liquid and / or a gas containing ammonia or having ammonia-forming potential.

Those skilled in the art will understand that the technical measures and advantages described above for method embodiments also apply to the corresponding system embodiments described below, mutatis mutandis.

According to a second aspect of the invention, a system is provided for the incineration of waste comprising nitrogen-bound components, the system comprising:

- a burner zone comprising a burner;

- a combustion zone;

- first feed means configured to provide a first stream of waste and second feed means for providing a second stream of waste, wherein:

- the first supply means are configured for introducing the first stream of waste into the burner zone;

- the burner is configured to oxidize the first stream of waste at a first temperature range in the burner zone such that NO x is formed;

- the second supply means are configured for introducing the second stream of waste into the incineration zone; and

mixing means configured to mix the NOx-containing oxidized waste and the second stream of waste in the combustion zone at a second temperature range such that the NOx concentration in the combustion zone is lowered.

In a preferred embodiment, the system further comprises:

BE2017 / 5802 · a conditioning zone configured to receive the mixture of oxidized waste and the second stream of waste from the combustion zone; and refrigerants configured to cool the mixture of oxidized waste and the second stream of waste in the conditioning zone at a third temperature range.

In a preferred embodiment, the system further comprises:

- a catalyst zone configured to receive the mixture of oxidized waste and the second stream of waste; and

- catalyst feed means configured to introduce a catalyst into the catalyst zone at a fourth temperature range such that NO x concentration in the catalyst zone is lowered.

In a preferred embodiment, the first temperature range is between 850 and 2000 ° C, preferably between 1000 and 1500 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C.

In a preferred embodiment, the second temperature range is between 800 and 1000 ° C, preferably between 850 and 950 ° C, more preferably between 875 and 940 ° C, and most preferably between 900 and 935 ° C.

In a preferred embodiment, the third temperature range is between 350 and 950 ° C, preferably between 400 and 935 ° C, more preferably between 450 and 850 ° C.

In a preferred embodiment, the fourth temperature range is between 150 and 650 ° C, preferably between 200 and 500 ° C, more preferably between 230 and 450 ° C, and most preferably between 320 and 380 ° C.

In a preferred embodiment, the system comprises a first checking device configured to check the amount of waste in the first stream based on a concentration of nitrogen-bound components in the second stream of waste.

In a preferred embodiment, the system comprises a second checking device configured to check the amount of waste in the first stream based on a concentration of NOx in the burner zone.

BE2017 / 5802

In a preferred embodiment, the system comprises a third control device configured to control the amount of waste in the second stream based on a concentration of nitrogen-bound components in the first stream of waste.

In a preferred embodiment, the system comprises a fourth control device configured to control the amount of algae in the second stream based on a concentration of NOx in the burner zone.

In a preferred embodiment, the mixing means comprise at least one mixing wall which is configured to transmit therethrough the NOx-containing oxidized waste from the burner zone in the direction of the combustion zone.

In a preferred embodiment, the system comprises additional feed means configured to introduce an additional amount of nitrogen-bound components into the combustion zone.

In a preferred embodiment, the system comprises a first temperature control device configured to control the first temperature range in the burner zone based on at least one of:

- a concentration of NOx in the burner zone;

- a concentration of NOx in the combustion zone;

- a concentration of NOx in the conditioning zone;

- a concentration of NOx in the catalyst zone;

- a concentration of nitrogen-bound components in the first stream of waste; and

- a concentration of nitrogen-bound components in the second stream of waste.

In a preferred embodiment, the system comprises a second temperature control device that is configured to control the second temperature range in the combustion zone based on at least one of:

- a concentration of NOx in the burner zone;

- a concentration of NOx in the combustion zone;

- a concentration of NOx in the conditioning zone;

- a concentration of NOx in the catalyst zone;

- a concentration of nitrogen-bound components in the first stream of waste; and

- a concentration of nitrogen-bound components in the second stream of waste.

BE2017 / 5802

In a preferred embodiment, the nitrogen-bound components comprise any of ammonia, urea, and nitrogen gas.

In a preferred embodiment, the waste comprising nitrogen-bound components is any of the following: a waste gas, a waste liquid, waste sludge, solid waste, or any combination thereof.

SHORT FIGURE DESCRIPTION

The attached figures are used to illustrate current non-limiting preferred embodiments of devices according to the present invention. The above described and other advantages of features and objects of the invention will become apparent and the invention will be better understood with reference to the detailed description when read together with the accompanying figures in which:

FIG. 1 is a schematic drawing of an exemplary embodiment of a waste incineration method comprising nitrogen-bound components;

FIG. 2 is a schematic drawing of another exemplary embodiment of a method for burning waste comprising nitrogen-bound components;

FIG. 3 is a schematic drawing of an alternative exemplary embodiment of a waste incineration system comprising nitrogen-bound components; and

FIG. 4 is a schematic drawing of yet another exemplary embodiment of a waste incineration system comprising nitrogen-bound components.

description of figures

The figures are only schematic and are non-limiting. In the figures, the size of some elements can be exaggerated and not drawn to scale for illustrative purposes. Reference numbers in the claims will not be considered as limiting the scope of protection. In the figures, the same reference numerals indicate the same or analogous elements.

FIG. 1 shows an exemplary embodiment of a method for the incineration of waste comprising nitrogen-bound components. The method includes the step S10 of providing a first stream of waste 110 and a second stream of waste 120. The first waste stream 110 and the second waste stream 120 are shown as coming from separate streams 110 and 120, however, in alternative embodiments, the first waste stream is 110 and second waste stream 120 both substroms from one common waste source. Therefore, depending on the actual origin of the first stream of waste 110 and the second stream of waste 120, they can

BE2017 / 5802 composition are substantially identical or mutually different. However, regardless of the exact composition of the first and second waste streams 110 and 120, both waste streams comprise nitrogen-bound components. The waste streams provided may take any form and may comprise any of a waste gas, a waste liquid, a waste sludge, and solid waste. Similar waste gases may be charged with hydrocarbons and may include vent gas, acid gas, and the like. The method further comprises step S20 of introducing the first stream of waste 110 into a burner zone 130. Depending on the shape of the waste, being solid, liquid or gas, different ways of introducing the first stream into the burner zone 130 of waste 110 which are known to the skilled person. During step S30, the first stream of waste 110 is oxidized in the burner zone 130 at a first temperature range T1 that is sufficiently high to form NOx from the nitrogen-bound components present in the first stream of waste 110. The first temperature T1 during S30 would between 850 and 2000 ° C, preferably between 1000 and 1500 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C. Preferably, the first waste stream 110 is oxidized under stoichiometric conditions. When NOx is formed during S30, the NOx-containing oxidized waste ends up in a combustion zone during step S40a. In step S40b, the second stream of waste 120 is fed into the combustion zone 140 such that the NOx-containing oxidized waste will react with the nitrogen-bound components, more particularly with ammonia and / or urea in the second waste stream 120 during step S50 to nitrogen gas and water. The second temperature T2 during S50 should be between 800 and 1000 ° C, preferably between 850 and 950 ° C, more preferably between 875 and 940 ° C, and most preferably between 900 and 935 ° C. Preferably, the amount of alval in the first stream of waste 110 is controlled in such a way that a stoichiometric ratio of NO x to nitrogen-bound components, such as ammonia, in the combustion zone 140 is between 1.0 and 1.5. The concentration of NOx and / or urea and / or ammonia can be measured at the end of the combustion process. Based on these measurement (s), the amount of nitrogen-bound components in the first waste stream 110 and / or the amount of urea / ammonia in the second waste stream 120 can be checked. The concentration of NOx can be measured by withdrawing an amount of flue gas from the corresponding zone 130 or 140 and having the amount withdrawn analyzed to calculate the amount of NOx. A flow rate of the extraction can be taken into account when calculating the amount of NOx. The amount of gas extracted can be processed before the actual analysis is carried out. The amount of gas extracted can, for example, be cooled and / or dried before it is sent to an analyzer to calculate the NOx concentration. A similar extraction can be carried out for measuring a concentration of urea and / or ammonia and / or other nitrogen-bound components.

BE2017 / 5802

Checking the amount of waste in the first stream 10 may include monitoring the composition of the first waste stream 110, and more particularly the concentration of nitrogen-bound components, and checking the flow rate of the first stream based on NOx levels in the burner zone, combustion zone, conditioning zone and / or catalyst zone.

Alternatively or in addition to controlling the amount of waste in the first stream of waste 110, the amount of waste in the second waste stream 120 can also be controlled in such a way that a stoichiometric ratio of NOx to nitrogen-bound components such as ammonia in the combustion zone between 1.0 and 1.5.

Checking the amount of waste in the second stream 120 may include monitoring the composition of the second waste stream 120, and more particularly the concentration of ammonia and / or urea, and checking the flow rate of the second stream based on of NOx levels in the burner zone 120 or combustion zone 140, conditioning zone 150 (see figure 2) and / or catalyst zone 160 (see figure 2).

When the first stream of waste 110 and second stream of waste 120 originate from a common waste source, the amount of waste, and more particularly the concentration of nitrogen-bound components in both streams of waste 110, 120, can split between the first stream 110 and the second stream 120 such that a correct amount of NOx and a correct amount of ammonia and / or urea are introduced into the combustion zone 140. The correct amounts of NOx and ammonia / urea can be determined based on the concentration of NOx at the end of the combustion process. The concentration of NOx at the end of the incineration process should be as low as possible and the quantities of waste, thus nitrogen-bound components, in the first and / or second streams of waste 110, 120 can be checked to ensure a minimum concentration of NOx on the end of the combustion process.

Due to the reaction of NOx in the oxidized waste with the nitrogen-bound components in the second waste stream 120, NOx levels will be significantly reduced. In other words, the method as shown in Figure 1 allows organic waste streams containing ammonia to be burned without the production of NOx fuel. Thus, there is no need for using a separately deNOx reagent such as ammonia or an additional catalyst, whereby the process as described requires less energy consumption compared to prior art solutions. In step S51, the resulting NOx-depleted gas can be emitted through an outlet. In exemplary embodiments, instead of ejecting the resulting gas, the resulting gas may be further processed as shown in Figure 2. The resulting NOx-depleted gas may additionally enter a waste heat recovery boiler where the gas is cooled to temperatures of

BE2017 / 5802 about 110-150 ° C. If halogens or sulfur or ash are present in the waste, an additional step can be performed in which the flue gas is cleaned, for example by means of a filter, scraper, or the like.

FIG. 2 shows a further exemplary embodiment of a method for burning gas comprising nitrogen-bound components. In addition to steps S10-S50 of the method as shown in Figure 1, the method according to Figure 2 comprises a further step S60 wherein the mixture of oxidized waste and the second stream of waste 120 is introduced into a conditioning zone 150. In the conditioning zone, the mixture of oxidized waste and the second stream of waste 120 is cooled during step S70 to reach a temperature within a third temperature range T3. The third temperature range T3 should be between 350 and 950 ° C, preferably between 400 and 935 ° C, more preferably between 450 and 850 ° C. After cooling, the mixture of oxidized waste and the second stream of ai 120 entered into a catalyst zone 160 during step S80. A catalyst is present in the catalyst zone 160 or is introduced during step S90, and the temperature is reduced to within a fourth temperature range T4 such that SCR can take place to further reduce the NO x concentration in the catalyst zone 160. In step S51, the NOx-depleted gas can be emitted through an outlet.

FIG. 3 shows an exemplary embodiment of a waste incineration system 200 comprising nitrogen-bound components. The system 200 comprises a burner zone 230 comprising a burner 231. In the burner zone 230, the burner 231 ensures that the temperature T1 is sufficiently high for oxidation to take place. The temperature T1 should be between 850 and 2000 ° C, preferably between 1000 and 1500 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C. The burner 231 can be any type of burner, as long as the temperature T1 in the burner zone 230 is guaranteed. The burner 231 is preferably a multi-fuel burner which burns ammonia gas and / or fuel gas. In the embodiment of Figure 3, a combustion zone 240 is placed directly next to the burner zone 230. First feed means 211 provide a first stream of refuse 210 and second feed means 221 provide a second stream of refuse 220. Although the first and second streams of refuse 210, 220 are shown as being two completely separate streams, it is obvious to those skilled in the art that both streams 210, 220 can come from one common waste source according to an alternative embodiment. Compositions of the waste streams 210, 220 can therefore be substantially identical or can be different, depending on the actual configuration of feed means 211 and 221. In each case, the first feed means 211 are configured to introduce the first stream into the burner zone 230

BE2017 / 5802 of waste 210, wherein the burner 231 is configured to oxidize the first stream of waste 210 at a sufficiently high temperature T1 such that NOx is formed. The NOx formed then travels from the burner zone 230 to the combustion zone 240. The second feed means 221 are configured to enter the second stream of waste 220 into the combustion zone 240. The oxidized waste containing NOx and the second waste waste stream into the combustion zone 240 will react at a second temperature T2 to form nitrogen gas and water. The second temperature T2 should be between 800 and 1000 ° C, preferably between 850 and 950 ° C, more preferably between 875 and 940 ° C, and most preferably between 900 and 935 ° C. Mixing means 290 are shown between the burner zone 230 and the combustion zone 240. These mixing means 290 may, for example, comprise a structural element such as a mixing wall. Alternatively, the mixing means 290 may be provided by means of an air stream within the burner zone 230 and / or combustion zone 240. Anyway, the mixing means 290 ensures mixing the NOx-containing oxidized waste with the second stream of waste 220 in the incineration zone 240 such that NO x concentration in the incineration zone 240 is lowered. Subsequently, resulting flue gases can be removed from the combustion zone 240 via outlet means 251. In exemplary embodiments, instead of outlet means 251 positioned in the combustion zone 240, the resulting gas in the combustion zone 240 can be further processed and additional zones are provided in addition to the burner zone 230. and combustion zone 240 as shown in the system of Figure 4.

FIG. 4 shows a further exemplary embodiment of a system 200 for the incineration of waste comprising nitrogen-bound components. The system 200 comprises a burner zone 230 comprising a burner 231 and a combustion zone 240 between two mixing walls 291, 292. In the embodiment of Figure 4, the first feed means 211a, 211b comprise two feed means 211a and 21 lb for providing two substroms 210a, 210b of the first stream of waste 210, respectively. Second feed means 221 are provided for providing a second stream of refuse 220. The first feed means 211 a, 21 lb are configured to introduce the substrates of refuse 210a, 210b into the burner zone 230 at positions above and below the burner 231 It is obvious to those skilled in the art that these waste substrates can be provided via other configurations such as, for example, a circular configuration positioned around the burner 231. It is further apparent to those skilled in the art that additional burners (not shown) may be provided in the burner zone 230 to ensure that the temperature T1 is sufficiently high and stable, such that the first waste streams 210a, 210b are oxidized in the burner zone 230. and NOx is formed. The first temperature T1 would be between 850 and 200 ° C, preferably between 1000 and 1500

BE2017 / 5802 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C. The curved arrows or swirls in the burner zone 230 indicate a preferred embodiment of the burner 231 in the burner zone 230 where air eddy currents are formed in the burner zone 230 such that the temperature T1 is kept stable and homogeneous and such that the incoming streams of waste 210a, 210b well mixed and burned. In addition, an air supply 232 is provided to inject air into the burner zone so as to promote the oxidation reaction in the burner zone 230. The second feed means 221 are configured to introduce the second stream of waste 220 into the incineration zone 240. In addition, mixing means 291, 292 are provided for mixing the NOx-containing oxidized waste and the second stream of waste into the combustion zone 240. at a second temperature T 2 such that NO x concertitration in the combustion zone 240 is lowered. The second temperature T2 should be between 800 and 1000 ° C, preferably between 850 and 950 ° C, more preferably between 875 and 940 ° C, and most preferably between 900 and 935 ° C. In the embodiment of Figure 4, the mixing means 291, 292 comprise a first mixing wall 291 and a second mixing wall 292. The first mixing wall 291 is placed between the burner zone 230 and the combustion zone 240. The second mixing wall 292 is placed between the combustion zone 240 and the combustion zone 240. conditioning zone 250. The conditioning zone 250 is configured to receive the mixture of oxidized waste and the second stream of waste from the combustion zone 240 and includes cooling means (not shown) adapted to cool the mixture of oxidized waste and the second stream of waste in the conditioning zone 250 at a third temperature range T3. The third temperature T3 should be between 350 and 950 ° C, preferably between 400 and 935 ° C, more preferably between 450 and 850 ° C. Cooled flue gases are removed from the conditioning zone 250 via exhaust means 251.

In the embodiment of Figure 4, additional feed means 220a are shown that are configured to inject an additional stream 221a into the combustion zone 240. In an embodiment, the additional stream 22.1a comprises waste comprising nitrogen-bound components and is from the first waste stream 210 and / or second waste stream 22.0. In an alternative embodiment, the additional stream 221a comprises ammonia gas and / or urea from a separate feed 22.0a. Either way, the additional stream 221a can be used to provide nitrogen-bound components that react with excess NOx present in the combustion zone 240.

In summary, the system 200 as shown in Figure 4 causes an ammonia-containing waste gas stream to be split into two streams of waste 210, 220. The first sub-stream of waste 210a, 210b is oxidized in the high temperature burner zone 230. This burner zone 230 becomes

BE2017 / 5802 kept at the correct temperature T1 by means of, for example, a multi-fuel burner which burns ammonia gas and / or fuel gas. The resulting NOx-containing gas passes along a mixing wall 291 before entering the combustion zone for the deNOx reaction. In the combustion zone 240, resulting NOx-containing gases are mixed with the remaining ammonia gases to obtain a selective non-catalytic reduction (SNCR) of NOx formed in the burner zone 230. In an exemplary embodiment, a reduction of NOx of about 50% is obtained in this combustion zone 240. The resulting combined gases are then cooled in the conditioning zone 250, for example, by injecting air. In a further embodiment, the cooled gases then enter the selective catalytic reduction (SCR) into a catalyst module (not shown) via outlet means 251, where the residual ammonia reacts with the residual NOx to obtain a further reduction of NOx.

As described above, the combustion system 200 trembles three zones 230, 240, 250.

In the burner zone 230, ammonia (NH 3) will be oxidized, along with all hydrocarbons, acids, mercaptans, and the like present. Vapors and waste air extracted are introduced into the burner zone 230, preferably in the vicinity of the burner 231. In a preferred embodiment, an auxiliary burner (not shown) is used to bring the system 200 and more particularly the burner zone 230 to the required temperature T1 and the burner zone 230 will be kept at this temperature T1. Preferably, a frequency speed controlled fan is used to provide the necessary amount of air to the burner 231. Preferably, this fan is controlled by a temperature control device of the burner zone 230 and / or combustion zone 240. The burner 231 may, for example, be operated at a lambda value of 1.1, which would result in a high diabetic temperature of around 1600 ° C and more. Thus, more air than necessary is injected into the burner zone 230 and / or combustion zone 240. This can be achieved by measuring a temperature in the burner zone 230 and / or combustion zone 240 and checking the speed of the fan in an appropriate manner. Alternatively, a fan operating at a constant speed and thereby generating a constant flow rate can be opened and closed to control the amount of air in the burner zone 230 and / or combustion zone 240.

In the combustion zone 240, the remaining part of the ammonia-containing waste gas 220 will be introduced by second feed means 221. The NH3 of the waste vapors will react with the NOx formed in the burner zone 230 to form nitrogen gas (N2) and water (H2O) . Preferably, the ratio of ammonia waste gas entering the burner zone 230 and the combustion zone 240 is controlled by means of a

BE2017 / 5802 flow rate control valve which, in turn, is controlled by the NOx measurement at the end of the combustion process, for example after the catalyst block. In addition to or alternatively, NO x measurements can be made in the burner zone 230, in the combustion zone 240, at the end of a cooling step, and / or in the conditioning zone 250.

In the conditioning zone 250, flue gases are mixed with cooling air to lower the temperature and achieve the requirements of the catalyst module. Cooling air is preferably added by means of electropneumatic air dampers, while the person skilled in the art can devise alternative ways of providing cooling air. In embodiments where no catalyst module is provided, flue gases are emitted to the atmosphere. When acids and / or ashes are present in the flue gases, an additional flue gas cleaning step can be added by means of a filter reactor, for example HCl, SOx and Dust filter, before the flue gas is emitted into the atmosphere.

In a further output gin form, a catalyst zone 160 is provided. For example, a catalyst module can be positioned in the path of the cooled flue gas stream. In this zone, the remaining ammonia reacts with the remaining NOx to form nitrogen and water. The catalyst also has a buffering effect since ammonia is absorbed on the surface before it reacts with NOx.

The temperature T1 in the burner zone 230 is typically much higher than 1000 ° C, due to the fact that the oxidation reaction of ammonia is most effective at temperatures above 1000 ° C. These high temperatures can also cause all odor components to be completely destroyed in an advantageous manner.

The temperature T 2 in the combustion zone 240 is preferably about 930 ° C, because the reaction of NO and / or NO 2 with ΝΉ 3 to form H 2 O and N 2 is most stable and effective at this temperature.

In a preferred embodiment, the combustion system 200 operates at a slight underpressure.

In one embodiment, the flue gases can be evacuated to a chimney after the combustion zone 240 by means of a flue gas extraction fan. This fan is preferably controlled on the basis of frequency velocity and ensures that zones 230, 240, 250 are in a state of slight underpressure.

BE2017 / 5802

While the principles of the invention have been described above with reference to specific embodiments, it will be understood that the description text is made by way of example and not as limiting the scope of protection defined by the appended claims.

Claims (10)

Conclusions A method for incinerating waste comprising nitrogen-bound components, the method comprising the steps of: - providing a first stream of waste and a second stream of waste; - introducing the first stream of waste into a burner zone; - oxidizing the first stream of waste at a first temperature range in the burner zone so that NO x is formed; - introducing oxidised waste containing NOx and the second stream of waste into a combustion zone; and - mixing the NOx-containing oxidized waste and the second stream of waste in the combustion zone at a second temperature range such that NOx concentration in the combustion zone is reduced. The method of claim 1, further comprising the steps of: - introducing the mixture of oxidized waste and the second stream of waste into a conditioning zone; and - cows the mixture of oxidized waste and the second stream of waste in the conditioning zone at a third temperature range. The method of claim 1 or 2, further comprising the steps of: - introducing the mixture of oxidized waste and the second waste stream into a catalyst zone; and - introducing a catalyst into the catalyst zone at a fourth temperature range such that NO x concentration in the catalyst zone is lowered. A method according to any one of the preceding claims, wherein the first temperature range is between 850 and 2000 ° C, preferably between 1000 and 1500 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C . 5 - a concentration of nitrogen-bound components in the second stream of waste. The system of any one of the preceding claims 18-32, wherein the nitrogen-bound components comprise any of ammonia, urea, and nitrogen gas. A method according to any one of the preceding claims, wherein the second temperature range is between 800 and 1000 ° C, preferably between 850 and 950 ° C, more preferably between 875 and 940 ° C, and most preferably between 900 and 935 ° C . The method of any one of claims 2-5, wherein the third temperature range is between 350 and 950 ° C, preferably between 400 and 935 ° C, more preferably between 450 and 850 ° C. 7. Method according to any of claims 3-6, wherein the fourth temperature range is between 150 and 650 ° C, preferably between 200 and 500 ° C, more preferably between 230 and 450 ° C, and most preferably between 320 and 380 ° C. A method according to any one of the preceding claims, wherein introducing the first stream of waste into the burner zone comprises checking the amount of waste in the first stream based on a concentration of nitrogen-bound components in the second stream of waste. A method according to any one of the preceding claims, wherein introducing the first stream of waste into the burner zone comprises checking the amount of waste in the first stream on the basis of a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone. A method according to any one of the preceding claims, wherein introducing the second stream of waste into the incineration zone comprises checking the amount of waste in the second stream based on a concentration of nitrogen-bound components in the first stream of waste. A method according to any one of the preceding claims, wherein introducing the second stream of waste into the combustion zone comprises checking the amount of waste in the second stream based on a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone. A method according to any one of the preceding claims, wherein introducing the NOx-containing oxidized waste into the combustion zone comprises forwarding the NOx-containing oxidized waste from the burner zone through at least one mixing wall in the direction of the combustion zone. A method according to any one of the preceding claims, comprising the step of introducing an additional amount of nitrogen-bound components into the combustion zone. A method according to any one of the preceding claims, further comprising the step of checking the first temperature range in the burner zone based on at least one of: - a concentration of NOx in the burner zone; BE2017 / 5802 BE2017 / 5802 - a concentration of NOx in the combustion zone; - a concentration of NOx in the conditioning zone; - a concentration of NOx in the catalyst zone; - a concentration of nitrogen-bound components in the first stream of waste; and - a concentration of nitrogen-bound components in the second stream of waste. The method of any one of the preceding claims, further comprising the step of checking the second temperature range in the combustion zone based on at least one of: - a concentration of NOx in the burner zone; - a concentration of NOx in the combustion zone; - a concentration of NOx in the conditioning zone; - a concentration of NOx in the catalyst zone; - a concentration of nitrogen-bound components in the first stream of waste; and - a concentration of nitrogen-bound components in the second stream of waste. The method of any one of the preceding claims, wherein the nitrogen-bound components comprise any of ammonia, urea, and nitrogen gas. A method according to any one of the preceding claims, wherein the waste comprising nitrogen-bound components is any of the following: a waste gas, a waste liquid, waste sludge, solid waste, or any combination thereof. 18. A waste incineration system comprising nitrogen-bound components, the system comprising the steps of: - a burner zone comprising a burner; - a combustion zone; - first feed means configured to provide a first stream of waste and second feed means for providing a second stream of waste, wherein: - the first supply means are configured for introducing the first stream of waste into the burner zone; - the burner is configured to oxidize the first stream of waste at a first temperature range in the burner zone such that NO x is formed; - the second supply means are configured for introducing the second stream of waste into the incineration zone; and BE2017 / 5802 mixing means configured to mix the NOx-containing oxidized waste and the second stream of waste in the combustion zone at a second temperature range such that the NOx concentration in the combustion zone is lowered. The system of claim 18, further comprising: - a conditioning zone configured to receive the mixture of oxidized waste and the second stream of waste from the combustion zone; and - cooling means configured to cool the mixture of oxidized waste and the second stream of waste in the conditioner zone at a third temperature range. The system of claim 18 or 19, further comprising: - a catalyst zone configured to receive the mixture of oxidized waste and the second stream of waste; and - catalyst feed means configured to introduce a catalyst into the catalyst zone at a fourth temperature range such that NO x concentration in the catalyst zone is lowered. A system according to any one of the preceding claims 18-20, wherein the first temperature range is between 850 and 2000 ° C, preferably between 1000 and 1500 ° C, more preferably between 1000 and 1250 ° C, and most preferably between 1050 and 1150 ° C. A system according to any one of the preceding claims 18-21, wherein the second temperature range is between 800 and 1000 ° C, preferably between 850 and 950 ° C, more preferably between 875 and 940 ° C, and most preferably between 900 and 935 ° C. The system of any one of claims 18 to 23, wherein the third temperature range is between 350 and 950 ° C, preferably between 400 and 935 ° C, more preferably between 450 and 850 ° C. The system of any one of claims 18 to 23, wherein the fourth temperature range is between 150 and 650 ° C, preferably between 200 and 500 ° C, more preferably between 230 and 450 ° C, and most preferably between 320 and 380 ° C. A system according to any one of the preceding claims 18-24, comprising a first checking device configured to check the amount of waste in the first stream based on a concentration of nitrogen-bound components in the second waste stream. BE2017 / 5802 26. A system according to any one of the preceding claims 18-25, comprising a second control device configured to control the amount of waste in the first stream on the basis of a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone . A system according to any one of the preceding claims 18-26, comprising a third checking device configured to check the amount of waste in the second stream based on a concentration of nitrogen-bound components in the first stream of waste. A system according to any one of the preceding claims 18-27, comprising a fourth checking device configured to check the amount of waste in the second stream based on a concentration of NOx in at least one of the burner zone, combustion zone, conditioning zone and catalyst zone . 29. System as claimed in any of the foregoing claims 18-28, wherein the mixing means comprise at least one mixing wall which is configured for forwarding through it the NOx-containing oxidised waste from the burner zone in the direction of the combustion zone. 30. System as claimed in any of the foregoing claims 18-29, comprising additional supply means which are configured for introducing an additional amount of nitrogen-bound components into the combustion zone. A system according to any one of the preceding claims 18-30, further comprising a first temperature control device configured to control the first temperature range in the burner zone based on at least one of: - a concentration of NOx in the burner zone; - a concentration of NOx in the combustion zone; - a concentration of NOx in the conditioning zone; - a concentration of NOx in the catalyst zone; - a concentration of nitrogen-bound components in the first stream of waste; and - a concentration of nitrogen-bound components in the second stream of waste. A system according to any of the preceding claims 18-31, further comprising a second temperature control device configured to control the second temperature range in the combustion zone based on at least one of: - a concentration of NOx in the burner zone; BE2017 / 5802 - a concentration of NOx in the combustion zone; - a concentration of NOx in the conditioning zone; - a concentration of NOx in the catalyst zone; - a concentration of nitrogen-bound components in the first stream of waste; and 34. A system according to any one of the preceding claims 18-33, wherein the waste comprising nitrogen-bound components is any of the following: honors waste gas, a waste liquid, waste sludge, solid waste, or any combination thereof.