Catalytic efficiency of flue gas filtration

Abstract

Some embodiments of the present disclosure relate to a method of regenerating at least one filter medium comprising: providing at least one filter medium, wherein the at least one filter medium comprises: at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; flowing a flue gas stream transverse to a cross-section of a filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium, wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and increasing an NO.sub.x removal efficiency of the at least one filter medium after removal of deposits.

Claims

1. A method comprising: providing at least one filter medium; wherein the at least one filter medium comprises: at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; flowing a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium, wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and increasing NO.sub.x removal efficiency of the at least one filter medium; wherein the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing an upstream NO.sub.2 concentration to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds, wherein increasing the upstream NO.sub.2 concentration to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds comprises introducing additional NO.sub.2 into the flue gas stream; and wherein the method regenerates the at least one filter medium.

2. The method of claim 1, wherein a temperature of the flue gas stream ranges from 160 C. to 280 C. during the flowing step.

3. The method of claim 1, wherein the flue gas stream further comprises Oxygen (O.sub.2), Water (H.sub.2O), Nitrogen (N.sub.2), Carbon Monoxide (CO), Sulfur Dioxide (SO.sub.2), Sulfur Trioxide (SO.sub.3), one or more hydrocarbons, or any combination thereof.

4. The method of claim 1, wherein flowing the flue gas stream transverse to the cross-section of the at least one filter medium comprises flowing the flue gas stream perpendicular to the cross-section of the at least one filter medium.

5. The method of claim 1, wherein the at least one filter medium is disposed within at least one filter bag, wherein the at least one filter bag is housed within at least one filter bag housing, and wherein the at least one catalyst material is in the form of catalyst particles.

6. The method of claim 5, wherein the at least one filter medium comprises: a porous protective layer; and a porous catalytic layer, wherein the porous catalytic layer comprises the catalyst particles.

7. The method of claim 6, wherein the porous protective layer of the at least one filter medium comprises a microporous layer, wherein the microporous layer comprises an expanded polytetrafluoroethylene (ePTFE) membrane.

8. The method of claim 6, wherein the porous catalytic layer of the at least one filter medium comprises at least one polymeric substrate.

9. The method of claim 6, wherein the porous catalytic layer comprises at least one ceramic substrate.

10. The method of claim 6, wherein the porous catalytic layer comprises polytetrafluorethylene (PTFE), poly(ethylene-co-tetrafluoroethylene) (ETFE), ultra-high molecular weight polyethylene (UHMWPE), polyparaxylylene (PPX), polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, fiberglass, or any combination thereof.

11. The method of claim 6 wherein the catalyst particles are enmeshed within the porous catalytic layer.

12. The method of claim 6, wherein the porous catalytic layer is in the form of a layered assembly comprising: a porous catalytic film; and at least one felt batt, wherein the at least one felt batt is positioned on at least one side of the porous catalytic film.

13. The method of claim 12, wherein the porous catalytic film comprises an expanded polytetrafluoroethylene (ePTFE) membrane.

14. The method of claim 12, wherein the at least one felt batt comprises: a polytetrafluoroethylene (PTFE) felt, a PTFE fleece, an expanded polytetrafluoroethylene (ePTFE) felt, an ePTFE fleece, a woven fluoropolymer staple fiber, a nonwoven fluoropolymer staple fiber, or any combination thereof.

15. The method of claim 1, wherein the at least one catalyst material comprises at least one of: Vanadium Monoxide (VO), Vanadium Trioxide (V.sub.2O.sub.3), Vanadium Dioxide (VO.sub.2), Vanadium Pentoxide (V.sub.2O.sub.5), Tungsten Trioxide (WO.sub.3), Molybdenum Trioxide (MoO.sub.3), Titanium Dioxide (TiO.sub.2), Silicon Dioxide (SiO.sub.2), Aluminum Trioxide (Al.sub.2O.sub.3), Manganese Oxide (MnO.sub.2), zeolites, or any combination thereof.

16. The method of any of claim 1, wherein ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 99% by mass of the at least one filter medium during the providing step.

17. The method of claim 1, wherein, after increasing the upstream NO.sub.2 concentration to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 98% by mass of the at least one filter medium.

18. The method of claim 1, wherein the increasing of the NO.sub.x removal efficiency comprises removing at least some of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium.

19. A method comprising: providing at least one filter medium wherein the at least one filter medium comprises at least one catalyst material; flowing a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from an upstream side of the filter medium to a downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); maintaining a constant NO.sub.x removal efficiency of the at least one filter medium; wherein the maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises: providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds, wherein providing the NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds comprises introducing additional NO.sub.2 into the flue gas stream; and controlling the NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.5% of the concentration of the flue gas stream; wherein the method cleans the flue gas stream.

20. A system comprising: at least one filter medium, wherein the at least one filter medium comprises: an upstream side; a downstream side; at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; at least one filter bag, wherein the at least one filter medium is disposed within the at least one filter bag; and at least one filter bag housing, wherein the at least one filter bag is disposed within the at least one filter bag housing; wherein the at least one filter bag housing is configured to receive a flow of a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from the upstream side of the at least one filter medium to the downstream side of the at least one filter medium, wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and wherein the system is configured to increase a NO.sub.x removal efficiency of the at least one filter medium when an upstream NO.sub.2 concentration is increased to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds, and wherein the upstream NO.sub.2 concentration is increased to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds by introducing additional NO.sub.2 into the flue gas stream.

21. A method comprising: providing at least one filter medium wherein the at least one filter medium comprises at least one catalyst material; flowing a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from an upstream side of the filter medium to a downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); maintaining an NO.sub.x removal efficiency of the at least one filter medium in an amount of at least 70% of an initial NO.sub.x efficiency by: providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds, wherein providing the NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds comprises introducing additional NO.sub.2 into the flue gas stream; and controlling NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.5% of the concentration of the flue gas stream wherein the method cleans the flue gas stream.

22. The method of claim 21, wherein maintaining the NO.sub.x removal efficiency comprises maintaining the NO.sub.x removal efficiency in a range of 70% to 99% of the initial NO.sub.x efficiency.

23. The method of claim 21, wherein maintaining of the NO.sub.x removal efficiency comprises increasing NO.sub.2 concentration periodically.

24. The method of claim 23, wherein increasing NO.sub.2 concentration periodically comprises increasing NO.sub.2 every 1 to 40,000 hours.

25. The method of claim 23, wherein increasing NO.sub.2 concentration periodically comprises increasing NO.sub.2 at constant time intervals.

26. The method of claim 23, wherein increasing NO.sub.2 concentration periodically comprises increasing NO.sub.2 at variable time intervals.

27. The method of claim 26, wherein the variable time intervals are random time intervals.

28. The method of claim 21, wherein providing the NO.sub.2 concentration comprises providing the NO.sub.2 concentration continuously.

29. The method of claim 28, further comprising providing the NO.sub.2 concentration continuously comprises providing NO.sub.2 at a flow rate of 2% to 99% of a total flow rate of the upstream NO.sub.x compounds.

Description

DRAWINGS

(1) Some embodiments of the disclosure are herein described, by way of example only, with reference to the accompanying drawings. With specific reference now to the drawings in detail, it is stressed that the embodiments shown are by way of example and for purposes of illustrative discussion of embodiments of the disclosure. In this regard, the description taken with the drawings makes apparent to those skilled in the art how embodiments of the disclosure may be practiced.

(2) FIGS. 1A-1D depict embodiments of an exemplary filter medium and according to the present disclosure.

(3) FIG. 2 depicts an exemplary NO.sub.x removal efficiency after in-situ flow-through regeneration by NO and NO.sub.2 gas mixture on an exemplary filter medium.

(4) FIG. 3 depicts an exemplary relative NO.sub.x removal efficiency after in-situ flow-through regeneration by NO and NO.sub.2 gas mixture on an exemplary filter medium.

(5) FIG. 4 depicts exemplary NO.sub.x concentrations, measured from a downstream side of an exemplary filter medium, during the in-situ flow through regeneration by an NO and NO.sub.2 mixture.

(6) FIG. 5 depicts an exemplary relative NO.sub.x removal efficiency after in-situ flow-through regeneration by NO, NO.sub.2 and NH.sub.3 gas mixture on an exemplary filter medium.

(7) FIG. 6 depicts an exemplary NO.sub.x concentration, measured from a downstream side of an exemplar filter medium, during the in-situ flow through regeneration by a mixture comprising NO, NO.sub.2, and NH.sub.3.

(8) FIG. 7 depicts an exemplary NO.sub.x removal efficiency after in-situ flow-by regeneration on an exemplary filter medium by a mixture comprising NO, NO.sub.2, and NH.sub.3.

(9) FIG. 8 depicts an exemplary NO.sub.x removal efficiency after in-situ flow-through regeneration on exemplary filter bags by a mixture comprising NO, NO.sub.2, and NH.sub.3.

(10) FIG. 9 depicts an example of long term NO.sub.x removal efficiency with SO.sub.2 and excess NO.sub.2 in the downstream.

(11) FIG. 10 depicts an example of long term NO.sub.x removal efficiency with SO.sub.2 but without excess NO.sub.2 in the downstream.

(12) FIG. 11 depicts an example of downstream NO.sub.2 concentration in an exemplary long term NO.sub.x removal efficiency measurement.

(13) FIG. 12 depicts an example of NO.sub.x removal efficiency and downstream NO.sub.2 concentration before, during and after in-situ flow-through regeneration by NO, NO.sub.2, and NH.sub.3 mixture with exposure to SO.sub.2.

(14) FIG. 13 depicts an example of NO.sub.x removal efficiency before, during and after in-situ flow-through regeneration (148 hours) by NO, NO.sub.2, and NH.sub.3 mixture with exposure to SO.sub.2.

(15) FIG. 14 depicts NO.sub.x removal efficiency with intermittent in-situ flow-through regeneration by an exemplary NO, NO.sub.2, and NH.sub.3 mixture with exposure to SO.sub.2.

DETAILED DESCRIPTION

(16) Among those benefits and improvements that have been disclosed, other objects and advantages of this disclosure will become apparent from the following description taken in conjunction with the accompanying figures. Detailed embodiments of the present disclosure are disclosed herein; however, it is to be understood that the disclosed embodiments are merely illustrative of the disclosure that may be embodied in various forms. In addition, each of the examples given regarding the various embodiments of the disclosure which are intended to be illustrative, and not restrictive.

(17) Throughout the specification and claims, the following terms take the meanings explicitly associated herein, unless the context clearly dictates otherwise. The phrases in one embodiment, in an embodiment, and in some embodiments as used herein do not necessarily refer to the same embodiment(s), though it may. Furthermore, the phrases in another embodiment and in some other embodiments as used herein do not necessarily refer to a different embodiment, although it may. All embodiments of the disclosure are intended to be combinable without departing from the scope or spirit of the disclosure.

(18) As used herein, the term based on is not exclusive and allows for being based on additional factors not described, unless the context clearly dictates otherwise. In addition, throughout the specification, the meaning of a, an, and the include plural references. The meaning of in includes in and on.

(19) All prior patents, publications, and test methods referenced herein are incorporated by reference in their entireties.

(20) As used herein, the term flow through means that a flue gas stream is flowed transverse to a cross section of the at least one filter medium, such that the flue gas stream passes through a cross section of the at least one filter medium. In some embodiments of a flow through configuration, the flue gas stream is flowed perpendicular to a cross-section of the at least one filter medium.

(21) As used herein, the term flow by means that the flue gas stream is not flowed transverse to a cross section of the at least one filter medium, such that the flue gas does not pass through the cross section of the at least one filter medium. In some embodiments of a flow by configuration, the flue gas stream is flowed parallel to a cross-section of the at least one filter medium.

(22) As used herein upstream refers to a location of a flue gas stream before entering a filter medium. In the flow through context, upstream may refer to the location of a flue gas stream before entering a cross section of a filter medium. In the flow by context, upstream may refer to the location of a flue gas stream before entering an enclosure (e.g., a housing, a filter bag, or other suitable enclosure described herein) that contains a filter medium.

(23) As used herein downstream refers to a location of a flue gas stream after exiting a filter medium. In the flow through context, downstream may refer to the location of a flue gas stream after exiting a cross section of a filter medium. In the flow by context, downstream may refer to the location of a flue gas stream after exiting an enclosure (e.g., a housing, a filter bag, or other suitable enclosure described herein) that contains a filter medium.

(24) As used herein, the term NO.sub.x compound refers to any oxide of nitrogen. In some non-limiting embodiments, NO.sub.x compound may specifically refer to gaseous oxides of nitrogen that are known environmental pollutants.

(25) As used herein, the term catalytic composite article set forth in the Examples refers to any material that includes a combination of at least one catalyst material and at least one additional material according to any embodiment described herein. The additional material is not limited to any particular type of material and may be, for example, a membrane, a felt batt, a ceramic substrate (including but not limited to a ceramic candle), a honeycomb substrate, a monolith substrate, or any combination thereof. The catalytic composite article may, in some non-limiting examples, be a porous catalytic film.

(26) Some embodiments of the present disclosure relate to a method of regenerating at least one filter medium.

(27) In some embodiments, the at least one filter medium comprises at least one catalyst material. In some embodiments, the at least one catalyst material comprises at least one of: Vanadium Monoxide (VO), Vanadium Trioxide (V.sub.2O.sub.3), Vanadium Dioxide (VO.sub.2), Vanadium Pentoxide (V.sub.2O.sub.5), Tungsten Trioxide (WO.sub.3), Molybdenum Trioxide (MoO.sub.3), Titanium Dioxide (TiO.sub.2), Silicon Dioxide (SiO.sub.2), Aluminum Trioxide (Al.sub.2O.sub.3), Manganese Oxide (MnO.sub.2), zeolites, or any combination thereof. In some embodiments, the at least one catalyst material is in the form of catalyst particles.

(28) In some embodiments, the at least one filter medium comprises an upstream side and a downstream side. In some embodiments, the at least one filter medium is disposed within at least one filter bag. In some embodiments, a plurality of filter mediums is disposed within a single filter bag. In some embodiments, the at least one filter bag is housed within at least one filter bag housing. In some embodiments, a plurality of filter bags is disposed within a single filter bag housing.

(29) In some embodiments, the one filter medium comprises a porous protective layer and a porous catalytic layer. In some embodiments, the porous catalytic layer comprises at least one catalyst material. In some embodiments, the at least one catalyst material is disposed on the porous catalytic layer. In some embodiments, the at least one catalyst material is within (e.g., embedded within) the porous catalytic layer.

(30) In some embodiments, the porous protective layer comprises a microporous layer. In some embodiments, the microporous layer comprises an expanded polytetrafluoroethylene (ePTFE) membrane.

(31) In some embodiments, the at least one catalyst material is adhered to the filter medium by at least one adhesive. In some embodiments, the at least one catalyst material is adhered to the porous catalytic layer by at least one adhesive. In some exemplary embodiments, the at least one filter medium is in the form of a filter bag, such that the adherence of the at least one catalyst material to the porous catalytic layer by the at least one adhesive form a coated filter bag. In some embodiments, the at least one catalyst material is in the form of catalyst particles, such that the coated filter bag is coated with the catalyst particles.

(32) In some embodiments, the at least one adhesive is chosen from polytetrafluoroethylene (PTFE), fluorinated ethylene propylene (FEP), high molecular weight polyethylene (HMWPE), high molecular weight polypropylene (HMWPP), perfluoroalkoxy alkane (PFA), polyvinylidene fluoride (PVDF), vinylidene fluoride (THV), chlorofluoroethylene (CFE), or any combination thereof. In some embodiments, the at least one adhesive is selected from the group consisting of polytetrafluoroethylene (PTFE), fluorinated ethylene propylene (FEP), high molecular weight polyethylene (HMWPE), high molecular weight polypropylene (HMWPP), perfluoroalkoxy alkane (PFA), polyvinylidene fluoride (PVDF), vinylidene fluoride (THV), chlorofluoroethylene (CFE), and any combination thereof.

(33) In some embodiments, the porous catalytic layer comprises at least one polymeric substrate. In some embodiments, the at least one polymeric substrate comprises a least one of: polytetrafluorethylene, poly(ethylene-co-tetrafluoroethylene), ultra-high molecular weight polyethylene, polyparaxylylene, polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, fiberglass, or any combination thereof. In some embodiments, the at least one polymeric substrate is selected from the group consisting of: polytetrafluorethylene, poly(ethylene-co-tetrafluoroethylene), ultra-high molecular weight polyethylene, polyparaxylylene, polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, fiberglass, and any combination thereof.

(34) In some embodiments, the porous catalytic layer includes at least one ceramic substrate. In some embodiments, the at least one ceramic substrate is in the form of a ceramic candle described herein. In some embodiments, the one ceramic substrate comprises ceramic fibers. In some embodiments, the ceramic fibers comprise alkali metal silicates, alkaline earth metal silicates, aluminosilicates, or any combination thereof.

(35) In some embodiments, the porous catalytic layer is in the form of a layered assembly comprising a porous catalytic film and one or more felt batts. In some embodiments, the one or more felt batts are positioned on at least one side of the porous catalytic film. In some embodiments, the porous catalytic film comprises the at least one catalyst material. In some embodiments, the at least one catalyst material is disposed on the porous catalytic film. In some embodiments, the at least one catalyst material is within (e.g., embedded within) the porous catalytic film.

(36) In some embodiments, the one or more felt batts comprise at least one of: a polytetrafluoroethylene (PTFE) felt, a PTFE fleece, an expanded polytetrafluoroethylene (ePTFE) felt, an ePTFE fleece, a woven fluoropolymer staple fiber, a nonwoven fluoropolymer staple fiber, or any combination thereof. In some embodiments, the one or more felt batts are selected from the group consisting of: a polytetrafluoroethylene (PTFE) felt, a PTFE fleece, an expanded polytetrafluoroethylene (ePTFE) felt, an ePTFE fleece, a woven fluoropolymer staple fiber, a nonwoven fluoropolymer staple fiber, and any combination thereof.

(37) In some embodiments, the porous catalytic film comprises a membrane. In some embodiments, the porous catalytic film comprises a polymer membrane. In some embodiments, the porous catalytic film comprises a fluoropolymer membrane and may be referred to as a porous catalytic fluoropolymer film. In some embodiments, the porous catalytic film comprises an expanded polytetrafluoroethylene (ePTFE) membrane.

(38) In some embodiments, the porous catalytic film comprises catalyst particles enmeshed within the ePTFE membrane. In some embodiments, the ePTFE membrane has a microstructure that includes nodes, fibrils, or any combination thereof. In some embodiments, the catalyst particles may be enmeshed into the microstructure. In some embodiments, the catalyst particles may be enmeshed into the nodes. In some embodiments, the catalyst particles may be enmeshed into the fibrils. In some embodiments, the catalyst particles may be enmeshed into the nodes and fibrils.

(39) In some embodiments, the at least one filter medium is in the form of a ceramic candle. In some embodiments, the ceramic candle comprises at least one ceramic material. In some embodiments, the least one ceramic material is chosen from: silica-aluminate, calcium-magnesium-silicate, calcium-silicate fibers, or any combination thereof. In some embodiments, catalyst particles form a coating on the at least one ceramic material.

(40) In some embodiments, the at least one filter medium may comprise any material configured to capture at least one of solid particulates, liquid aerosols, or any combination thereof from a flue gas stream. In some embodiments, the at least one filter medium is in the form of at least one of: a filter bag, a honeycomb, a monolith or any combination thereof.

(41) In some embodiments, the at least filter medium comprises ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof. In some embodiments, ABS deposits are disposed on the at least one catalyst material of the at least one filter medium. In some embodiments, ABS deposits are disposed within the at least one catalyst material of the at least one filter medium.

(42) In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.1% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 1% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 10% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 25% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 50% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 75% to 99% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 95% to 99% by mass of the at least one filter medium during the providing step.

(43) In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 95% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 75% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 50% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 25% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 10% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 1% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 0.01% to 0.1% by mass of the at least one filter medium during the providing step.

(44) In some embodiments, the ABS deposits are present in a concentration ranging from 0.1% to 95% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 1% to 75% by mass of the at least one filter medium during the providing step. In some embodiments, the ABS deposits are present in a concentration ranging from 10% to 50% by mass of the at least one filter medium during the providing step.

(45) In some embodiments, the method of regenerating at least one filter medium comprises flowing a flue gas stream through the at least one filter medium (i.e., transverse to a cross-section of the at least one filter medium), such that the flue gas stream passes through the cross section of the at least one filter medium. In some embodiments, the flue gas stream is flowed from an upstream side to a downstream side of the at least one filter medium. In some embodiments, the flue gas stream is flowed perpendicular to a cross-section of the at least one filter medium.

(46) In some embodiments, the method of regenerating at least one filter medium comprises flowing a flue gas stream by the at least one filter medium (i.e., non-transverse to a cross-section of the at least one filter medium), such that the flue gas stream does not pass through the cross section of the at least one filter medium. In some embodiments, the flue gas stream is flowed parallel to a cross-section of the at least one filter medium.

(47) In some embodiments, the temperature of the flue gas stream ranges from 160 C. to 280 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 175 C. to 280 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 200 C. to 280 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 225 C. to 280 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 250 C. to 280 C. during the flowing step.

(48) In some embodiments, the temperature of the flue gas stream ranges from 160 C. to 250 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 160 C. to 225 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 160 C. to 200 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 160 C. to 175 C. during the flowing step.

(49) In some embodiments, the temperature of the flue gas stream ranges from 175 C. to 250 C. during the flowing step. In some embodiments, the temperature of the flue gas stream ranges from 200 C. to 225 C. during the flowing step.

(50) In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 170 C. to 450 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 200 C. to 450 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 250 C. to 450 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 300 C. to 450 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 350 C. to 450 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 400 C. to 450 C. during the flowing step.

(51) In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 170 C. to 400 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 170 C. to 350 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 170 C. to 300 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 170 C. to 250 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 170 C. to 200 C. during the flowing step.

(52) In some embodiments, such as embodiments where the at least one filter medium is in the form of a or comprises ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 200 C. to 400 C. during the flowing step. In some embodiments, such as embodiments where the at least one filter medium is in the form of or comprises a ceramic substrate (e.g., a ceramic candle), the temperature of the flue gas stream ranges from 250 C. to 350 C. during the flowing step.

(53) In some embodiments, the flue gas stream comprises NO.sub.x compounds comprising. In some embodiments, the NO.sub.x compounds comprise Nitric Oxide (NO) and Nitrogen Dioxide (NO.sub.2). In some embodiments, the flue gas stream further comprises at least one of Oxygen (O.sub.2), Water (H.sub.2O), Nitrogen (N.sub.2), Carbon Monoxide (CO), Sulfur Dioxide (SO.sub.2), Sulfur Trioxide (SO.sub.3), one or more hydrocarbons, or any combination thereof.

(54) In some embodiments, the method of regenerating at least one filter medium comprises increasing NO.sub.x removal efficiency of the at least one filter medium.

(55) In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 5% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 10% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 25% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 50% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 75% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 95% to 99% of a total concentration of the NO.sub.x compounds.

(56) In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 95% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 75% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 50% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 25% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 10% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 2% to 5% of a total concentration of the NO.sub.x compounds.

(57) In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 5% to 95% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 10% to 75% of a total concentration of the NO.sub.x compounds. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing NO.sub.2 concentration to a range from 25% to 50% of a total concentration of the NO.sub.x compounds.

(58) In some embodiments, the concentration of NO.sub.2 is increased by introducing at least one oxidizing agent to the flue gas stream. In some embodiments, the at least one oxidizing agent is chosen from: hydrogen peroxide (H.sub.2O.sub.2), ozone (O.sub.3), hydroxyl radical or any combination thereof. In some embodiments, the at least one oxidizing agent is selected from the group consisting of: H.sub.2O.sub.2, O.sub.3, hydroxyl radical, and any combination thereof.

(59) In some embodiments, the concentration of NO.sub.2 is increased by introducing additional NO.sub.2 into the flue gas stream.

(60) In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding ammonia (NH.sub.3) in a concentration ranging from 0.0001% to 0.5% of the concentration of the flue gas stream. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding NH.sub.3 in a concentration ranging from 0.001% to 0.5% of the concentration of the flue gas stream. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding ammonia NH.sub.3 in a concentration ranging from 0.01% to 0.5% of the concentration of the flue gas stream. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding ammonia NH.sub.3 in a concentration ranging from 0.1% to 0.5% of the concentration of the flue gas stream.

(61) In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding NH.sub.3 in a concentration ranging from 0.0001% to 0.1% of the concentration of the flue gas stream. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding NH.sub.3 in a concentration ranging from 0.0001% to 0.05% of the concentration of the flue gas stream. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding NH.sub.3 in a concentration ranging from 0.0001% to 0.005% of the concentration of the flue gas stream.

(62) In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding NH.sub.3 in a concentration ranging from 0.005% to 0.1% of the concentration of the flue gas stream. In some embodiments, the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding NH.sub.3 in a concentration ranging from 0.005% to 0.05% of the concentration of the flue gas stream.

(63) In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 0.5% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 1% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 5% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 10% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 25% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 50% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 75% higher after the increasing step than during the providing step. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is at least 100% higher after the increasing step than during the providing step.

(64) In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing at least some of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing at least 10% of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing at least 25% of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing at least 50% of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing at least 75% of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing at least 95% of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. In some embodiments, the increasing of the NO.sub.x removal efficiency comprises removing all of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium.

(65) In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 90% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 50% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 20% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 10% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 5% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 1% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 0.1% by mass of the at least one filter medium.

(66) In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.1% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 1% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 5% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 10% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 20% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 50% to 98% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 90% to 98% by mass of the at least one filter medium.

(67) In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.1% to 90% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 1% to 50% by mass of the at least one filter medium. In some embodiments, after the increasing step, ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 5% to 20% by mass of the at least one filter medium.

(68) Some embodiments of the present disclosure relate to a method of cleaning a flue gas stream. In some embodiments, the method of cleaning the flue gas stream may comprise flowing a flue gas stream through a filter medium as described herein, (i.e., transverse to a cross-section of a filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium).

(69) In some embodiments of the method of cleaning the flue gas stream, the flue gas stream may comprise NO.sub.x compounds. In some embodiments, the NO.sub.x compounds may comprise Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2). In some embodiments, the flue gas stream may further comprise Sulfur Dioxide (SO.sub.2) and Ammonia (NH.sub.3).

(70) In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 1 mg/m.sup.3 based on a total volume of the flue gas stream. In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 2 mg/m.sup.3 based on a total volume of the flue gas stream. In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 5 mg/m.sup.3 based on a total volume of the flue gas stream. In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 10 mg/m.sup.3 based on a total volume of the flue gas stream. In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 25 mg/m.sup.3 based on a total volume of the flue gas stream. In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 50 mg/m.sup.3 based on a total volume of the flue gas stream. In some embodiments, the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 100 mg/m.sup.3 based on a total volume of the flue gas stream.

(71) In some embodiments of the method of cleaning the flue gas stream, the method may include maintaining a constant NO.sub.x removal efficiency of the at least one filter medium. In some embodiments of the method of cleaning the flue gas stream, the method may include maintaining NO.sub.x removal efficiency of the at least one filter medium that does not vary by more than 1%. In some embodiments of the method of cleaning the flue gas stream, the method may include maintaining NO.sub.x removal efficiency of the at least one filter medium that does not vary by more than 5%. In some embodiments of the method of cleaning the flue gas stream, the method may include maintaining NO.sub.x removal efficiency of the at least one filter medium that does not vary by more than 10%.

(72) In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 5% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 10% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 25% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 50% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 75% to 99% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 95% to 99% of a total concentration of the NO.sub.x compounds.

(73) In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 95% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 75% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 50% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 25% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 10% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 5% of a total concentration of the NO.sub.x compounds.

(74) In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 5% to 95% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium in a range from 10% to 75% of a total concentration of the NO.sub.x compounds. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 25% to 50% of a total concentration of the NO.sub.x compounds.

(75) In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.5% of the concentration of the flue gas stream. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.001% to 0.5% of the concentration of the flue gas stream. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.01% to 0.5% of the concentration of the flue gas stream. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.1% to 0.5% of the concentration of the flue gas stream.

(76) In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.1% of the concentration of the flue gas stream. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.01% of the concentration of the flue gas stream. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.001% of the concentration of the flue gas stream.

(77) In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.001% to 0.1% of the concentration of the flue gas stream. In some embodiments, maintaining a constant NO.sub.x removal efficiency of the at least one filter medium may include controlling an NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.01% to 0.1% of the concentration of the flue gas stream.

(78) In some embodiments NO.sub.x efficiency is maintained in an amount of at least 70% of an initial NO.sub.x efficiency. In some embodiments NO.sub.x efficiency is maintained in an amount of at least 75% of an initial NO.sub.x efficiency. In some embodiments NO.sub.x efficiency is maintained in an amount of at least 80% of an initial NO.sub.x efficiency. In some embodiments NO.sub.x efficiency is maintained in an amount of at least 85% of an initial NO.sub.x efficiency. In some embodiments NO.sub.x efficiency is maintained in an amount of at least 90% of an initial NO.sub.x efficiency. In some embodiments NO.sub.x efficiency is maintained in an amount of at least 95% of an initial NO.sub.x efficiency. In some embodiments NO.sub.x efficiency is maintained in an amount of at least 99% of an initial NO.sub.x efficiency.

(79) In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 99% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 75% to 99% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 80% to 99% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 85% to 99% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 90% to 99% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 95% to 99% of the initial NO.sub.x efficiency.

(80) In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 95% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 90% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 85% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 80% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 75% of the initial NO.sub.x efficiency.

(81) In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 75% to 95% of the initial NO.sub.x efficiency. In some embodiments, the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 80% to 90% of the initial NO.sub.x efficiency.

(82) In some embodiments, NO.sub.x efficiency is maintained by increasing NO.sub.2. In some embodiments, NO.sub.2 is increased periodically. In some embodiments, NO.sub.2 is increased continuously. In some embodiments, the periodic addition of NO.sub.2 occurs at constant time intervals. In some embodiments, the periodic addition of NO.sub.2 occurs at variable time intervals. In some embodiments, the periodic addition of NO.sub.2 occurs at random time intervals.

(83) In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 10 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 100 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1,000 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 5,000 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 10,000 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 20,000 to 40,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 30,000 to 40,000 hours.

(84) In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 30,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 20,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 10,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 5,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 1,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 100 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 10 hours.

(85) In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 10 to 30,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 100 to 20,000 hours. In some embodiments, the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1,000 to 5,000 hours.

(86) In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 5% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 10% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 20% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 30% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 40% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 50% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 60% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 70% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 80% to 99% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 95% to 99% of a total flow rate of the upstream NO.sub.x compounds.

(87) In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 95% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 90% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 80% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 70% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 60% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 50% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 40% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 30% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 20% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 10% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 5% of a total flow rate of the upstream NO.sub.x compounds.

(88) In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 5% to 95% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 10% to 90% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 20% to 80% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 30% to 70% of a total flow rate of the upstream NO.sub.x compounds. In some embodiments, the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 40% to 60% of a total flow rate of the upstream NO.sub.x compounds.

(89) FIGS. 1A-1D depict embodiments of an exemplary filter medium according to the present disclosure.

(90) Referring to FIG. 1A, at least one filter medium 101 may be housed in at least one filter bag 100. A flue gas stream 102 may flow through the at least one filter medium 101 by passing through cross section A. Once the flue gas stream 102 flows through the at least one filter medium 101, the flue gas stream 102 may flow by the at least one filter bag, as indicated by the vertically oriented arrows.

(91) FIG. 1B depicts an exemplary filter medium 101 according to some embodiments of the present disclosure. As shown in FIG. 1B, a flue gas stream 102, which may comprise NO.sub.x compounds and solid particulates 107, may flow through cross section A from an upstream side 103 of the filter medium 101 to a downstream side 104 of the filter medium. While not shown, the upstream side 103 of the filter medium 101 may, in some embodiments, correspond to an outside of a filter bag, such as filter bag 100. Likewise, downstream side 104 of the filter medium 101 may correspond to an inside of a filter bag, such as filter bag 100. In some embodiments, filter medium 101 may include at least one protective membrane 106 and one or more felt batts 108 on at least one of: the upstream side 103 the of the filter medium 101, the downstream side 104 the of the filter medium 101, or any combination thereof. In some embodiments, the one or more felt batts 108 may be positioned on a porous catalytic film 105. In some embodiments, the combination of the one or more felt batts 108 and the porous catalytic film 105 may be referred to as a porous catalytic layer (not shown in FIG. 1B).

(92) FIG. 1C depicts a non-limiting exemplary embodiment of the porous catalytic film 105. As shown, porous catalytic film 105 may include catalyst particles 109 on at least one surface of the porous catalytic film 105. ABS deposits 110 may be disposed on the surface of the catalyst particles 109.

(93) FIG. 1D depicts an additional non-limiting exemplary embodiment of a filter medium 101. As shown, filter medium 101 may comprise a porous catalytic layer 111. In some non-limiting embodiments, filter medium 101 may take the form of a filter bag. In some embodiments the porous catalytic layer 111 may be coated with a catalyst material (not shown in FIG. 1D) such as catalyst particles. In some embodiments, the catalyst material may be attached to the porous catalytic layer 111 by one or more adhesives described herein (not shown). In some embodiments, the filter medium 101 may include a porous protective membrane 106.

(94) At least some non-limiting aspects of the present disclosure will now be described with reference to the following numbered embodiments hereinafter designated as [E1, E2, E3, E4 . . . ]: E1. A method comprising: providing at least one filter medium; wherein the at least one filter medium comprises: at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; flowing a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and increasing NO.sub.x removal efficiency of the at least one filter medium; wherein the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing an upstream NO.sub.2 concentration to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds,
wherein the method regenerates the at least one filter medium. E2. A method comprising: providing at least one filter medium; wherein the at least one filter medium comprises: at least one catalyst material; and ammonium bisulfate (ABS), ammonium sulfate (AS), or any combination thereof; flowing a flue gas stream through or by the at least one filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); increasing NO.sub.x removal efficiency of the at least one filter medium; wherein the increasing of the NO.sub.x removal efficiency of the at least one filter medium comprises increasing an upstream NO.sub.2 concentration to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds; wherein the increasing of the NO.sub.x removal efficiency of the at least one filter medium further comprises adding ammonia (NH.sub.3) in a concentration ranging from 0.0001% to 0.5% of the concentration of the flue gas stream;
wherein the method regenerates the at least one filter medium. E3. The method of any of the preceding embodiments or any combination thereof, wherein the temperature of the flue gas stream ranges from 160 C. to 280 C. during the flowing step. E4. The method of any of the preceding embodiments, or any combination thereof, wherein the flue gas stream further comprises at least one of Oxygen (O.sub.2), Water (H.sub.2O), Nitrogen (N.sub.2), Carbon Monoxide (CO), Sulfur Dioxide (SO.sub.2), Sulfur Trioxide (SO.sub.3), one or more hydrocarbons, or any combination thereof. E5. The method of embodiment 2, wherein the flue gas stream is flowed transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium. E6. The method of embodiment 2, wherein the flue gas stream is not flowed transverse to a cross-section of the at least one filter medium, such that the flue gas stream does not pass through the cross section of the at least one filter medium. E7. The method of embodiment 1, 3-5, or any combination thereof, wherein the flue gas stream is flowed perpendicular to a cross-section of the at least one filter medium. E8. The method of embodiment 6, wherein the flue gas stream is flowed parallel to a cross-section of the at least one filter medium. E9. The method of embodiments 1, 3-5, 7, or any combination thereof, wherein the at least one filter medium is disposed within at least one filter bag, wherein the at least one filter bag is housed within at least one filter bag housing, and wherein the at least one catalyst material is in the form of catalyst particles. E10. The method of any of embodiments 1, 3-5, 7, 9, or any combination thereof, wherein the at least one filter medium comprises a porous protective layer and a porous catalytic layer, wherein the porous catalytic layer comprises the at least one catalyst material. E11. The method of embodiment 10, wherein the porous protective layer comprises a microporous layer, wherein the microporous layer comprises an expanded polytetrafluoroethylene (ePTFE) membrane. E12. The method of any of the preceding embodiments wherein the at least one catalyst material is adhered to the filter medium by at least one adhesive. E13. The method of embodiment 12, wherein the at least one adhesive is chosen from polytetrafluoroethylene (PTFE), fluorinated ethylene propylene (FEP), high molecular weight polyethylene (HMWPE), high molecular weight polypropylene (HMWPP), perfluoroalkoxy alkane (PFA), polyvinylidene fluoride (PVDF), vinylidene fluoride (THV), chlorofluoroethylene (CFE), or any combination thereof. E14. The method of embodiments, 9-10, 12, or any combination thereof, wherein the porous catalytic layer comprises at least one polymeric substrate. E15. The method of embodiment 14, wherein the at least one polymeric substrate comprises a least one of: polytetrafluorethylene, poly(ethylene-co-tetrafluoroethylene), ultra-high molecular weight polyethylene, polyparaxylylene, polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, fiberglass, or any combination thereof. E16. The method of embodiments, 9-10, 12, wherein the porous catalytic layer includes at least one ceramic substrate. E17. The method of embodiment 16, wherein the at least one ceramic substrate comprises ceramic fibers, wherein the ceramic fibers comprise, alkali metal silicates, alkaline earth metal silicates, aluminosilicates, or any combination thereof. E18. The method of embodiments 9-10 or any combination thereof, wherein the porous catalytic layer is in the form of a layered assembly comprising a porous catalytic film and one or more felt batts, wherein the one or more felt batts are positioned on at least one side of the porous catalytic film. E19. The method of embodiment 18, wherein the one or more felt batts comprise at least one of: a polytetrafluoroethylene (PTFE) felt, a PTFE fleece, an expanded polytetrafluoroethylene (ePTFE) felt, an ePTFE fleece, a woven fluoropolymer staple fiber, a nonwoven fluoropolymer staple fiber, or any combination thereof. E20. The method of embodiment 18, 19, or any combination thereof, wherein the porous catalytic film comprises an expanded polytetrafluoroethylene (ePTFE) membrane. E21. The method of embodiments 10, 18-19, or any combination thereof, wherein the catalyst particles are enmeshed within the porous catalytic layer. E22. The method of embodiments 10, 18-20, or any combination thereof, wherein the porous catalytic layer comprises a least one of: polytetrafluorethylene (PTFE), poly(ethylene-co-tetrafluoroethylene) (ETFE), ultra-high molecular weight polyethylene (UHMWPE), polyparaxylylene (PPX), polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, fiberglass, or any combination thereof. E23. The method of embodiments 1-8, or any combination thereof, wherein the at least one filter medium is in the form of a ceramic candle, wherein the ceramic candle comprises at least one ceramic material. E24. The method of embodiment 16, 17, 22, or any combination thereof, wherein the temperature of the flue gas stream ranges from 170 C. to 450 C. during the flowing step. E25. The method of embodiment 23, 24, or any combination thereof, wherein the least one ceramic material is chosen from: silica-aluminate, calcium-magnesium-silicate, calcium-silicate fibers, or any combination thereof. E26. The method of embodiments 24-25, or any combination thereof, wherein the at least one catalyst is in the form of catalyst particles, wherein the catalyst particles form a coating on the at least one ceramic material. E27. The method of any of the preceding embodiments or any combination thereof, wherein the at least one catalyst material comprises at least one of: Vanadium Monoxide (VO), Vanadium Trioxide (V.sub.2O.sub.3), Vanadium Dioxide (VO.sub.2), Vanadium Pentoxide (V.sub.2O.sub.5), Tungsten Trioxide (WO.sub.3), Molybdenum Trioxide (MoO.sub.3), Titanium Dioxide (TiO.sub.2), Silicon Dioxide (SiO.sub.2), Aluminum Trioxide (Al.sub.2O.sub.3), Manganese Oxide (MnO.sub.2), zeolites, or any combination thereof. E28. The method of any of the preceding embodiments or any combination thereof, wherein ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 99% by mass of the at least one filter medium during the providing step. E29. The method of any of the preceding embodiments or any combination thereof, wherein ABS deposits are disposed on the catalyst material of the at least one filter medium in a concentration ranging from 0.01% to 98% by mass of the at least one filter medium after the increasing step. E30. The method of any of the preceding embodiments or any combination thereof, wherein the concentration of NO.sub.2 is increased by introducing at least one oxidizing agent to the flue gas stream. E31. The method of embodiment 21, wherein the at least one oxidizing agent is chosen from: hydrogen peroxide (H.sub.2O.sub.2), ozone (O.sub.3), hydroxyl radical, or any combination thereof. E32. The method of embodiment 21, wherein the concentration of NO.sub.2 is increased by introducing additional NO.sub.2 into the flue gas stream. E33. The method of embodiments 1, 3, 4, 7, 9-32, or any combination thereof further comprising adding NH.sub.3 in a concentration ranging from 0.0001% to 0.5% of the concentration of the flue gas stream. E34. The method of any of the preceding embodiments or any combination thereof, wherein the NO.sub.x removal efficiency of the at least one filter medium is at least 0.5% higher after the increasing step than during the providing step. E35. The method of embodiment 2, wherein the at least one filter medium is in the form of at least one of: a filter bag, a honeycomb structure, a monolith structure or any combination thereof. E36. The method of any of the preceding embodiments or any combination thereof, wherein the increasing of the NO.sub.x removal efficiency comprises removing at least some of the ABS deposits, the AS deposits, or any combination thereof, from the at least one filter medium. E37. A method comprising: providing at least one filter medium wherein the at least one filter medium comprises at least one catalyst material; flowing a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from an upstream side of the filter medium to a downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); maintaining a constant NO.sub.x removal efficiency of the at least one filter medium; wherein the maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises: providing NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds; and controlling NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.5% of the concentration of the flue gas stream
wherein the method cleans the flue gas stream. E38. The method of embodiment 37, wherein the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 1 mg/m.sup.3 based on a total volume of the flue gas stream. E39. A method comprising: providing at least one filter medium wherein the at least one filter medium comprises at least one catalyst material; flowing a flue gas stream by a cross-section of the at least one filter medium, such that the flue gas stream is flowed parallel to a cross-section of the at least one filter medium from an upstream side of the filter medium to a downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); maintaining a constant NO.sub.x removal efficiency of the at least one filter medium; wherein the maintaining a constant NO.sub.x removal efficiency of the at least one filter medium comprises: providing NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds; and controlling NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.5% of the concentration of the flue gas stream
wherein the method cleans the flue gas stream. E40. The method of embodiment 39, wherein the SO.sub.2, NH.sub.3, and NO.sub.x compounds are present in an amount of at least 1 mg/m.sup.3 based on a total volume of the flue gas stream. E41. The method of embodiment 39, wherein the at least one filter medium is in the form of at least one of: a honeycomb structure, a monolith structure or any combination thereof. E42. A filter medium comprising: an upstream side; a downstream side; at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; wherein the filter medium is configured to receive a flow of a flue gas stream transverse to a cross-section of the filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from the upstream side of the filter medium to the downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and wherein the at least one filter medium is configured to increase an NO.sub.x removal efficiency of the at least one filter medium when an upstream NO.sub.2 concentration is increased to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds. E43. The filter medium of embodiment 42, wherein, the at least one filter medium is configured to further increase an NO.sub.x removal efficiency of the at least one filter medium when ammonia (NH.sub.3) is added in a concentration ranging from 0.0001% to 0.5% of the concentration of the flue gas stream. E44. A filter medium comprising: an upstream side; a downstream side; and at least one catalyst material; wherein the filter medium is configured to receive a flow of a flue gas stream transverse to a cross-section of the filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from the upstream side of the filter medium to the downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); wherein the at least one filter medium is configured to maintain a constant NO.sub.x removal efficiency of the at least one filter medium when: an NO.sub.2 concentration, measured from the upstream side of the filter medium, is provided in a range from 2% to 99% of a total concentration of the NO.sub.x compounds; and an NO.sub.2 concentration, measured from the downstream side of the filter medium, is controlled to a range of from 0.0001% to 0.5% of the total concentration of the flue gas stream. E45. A filter medium comprising: an upstream side; a downstream side; and at least one catalyst material; wherein the filter medium is configured to receive a flow of a flue gas stream by a cross-section of the filter medium, such that the flue gas stream is not flowed transverse to a cross-section of the at least one filter medium from an upstream side of the filter medium to a downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); wherein the at least one filter medium is configured to maintain a constant NO.sub.x removal efficiency of the at least one filter medium when: an NO.sub.2 concentration, measured from the upstream side of the filter medium, is provided in a range from 2% to 99% of a total concentration of the NO.sub.x compounds; and an NO.sub.2 concentration, measured from the downstream side of the filter medium, is controlled to a range of from 0.0001% to 0.5% of the total concentration of the flue gas stream. E46. A system comprising: at least one filter medium, wherein the at least one filter medium comprises: an upstream side; a downstream side; at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; at least one filter bag, wherein the at least one filter medium is disposed within the at least one filter bag; and at least one filter bag housing, wherein the at least one filter bag is disposed within the at least one filter bag housing; wherein the at least one filter bag housing is configured to receive a flow of a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from the upstream side of the at least one filter medium to the downstream side of the at least one filter medium, wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and wherein the system is configured to increase an NO.sub.x removal efficiency of the at least one filter medium when an upstream NO.sub.2 concentration is increased to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds. E47. A filter bag housing comprising: a filter medium, wherein the filter medium comprises: an upstream side; a downstream side; at least one catalyst material; and ammonium bisulfate (ABS) deposits, ammonium sulfate (AS) deposits, or any combination thereof; and a filter bag, wherein the filter medium is disposed within the filter bag; wherein the filter bag is disposed within the filter bag housing; wherein the filter bag housing is configured to receive a flow of a flue gas stream transverse to a cross-section of the filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from the upstream side of the filter medium to the downstream side of the filter medium, wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); and wherein the filter bag housing is configured to increase an NO.sub.x removal efficiency of the at least one filter medium when an upstream NO.sub.2 concentration is increased to a range from 2% to 99% of a total concentration of the upstream NO.sub.x compounds. E48. The method of embodiments 1 to 41 or any combination thereof, wherein NO.sub.2 is added to the flue gas stream periodically, so as to maintain the NO.sub.x removal efficiency in an amount of at least 70% of an initial NO.sub.x efficiency. E49. The method of embodiment 48, wherein the periodic addition of NO.sub.2 comprises increasing NO.sub.2 every 1 to 40,000 hours. E50. The method of embodiment 48, 49, or any combination thereof, wherein the periodic addition occurs at constant time intervals. E51. The method of embodiment 48, 49, or any combination thereof, wherein the periodic addition occurs at variable time intervals. E52. The method of embodiment 51, wherein variable time intervals are random time intervals. E53. The method of embodiments 1 to 41 or any combination thereof, wherein NO.sub.2 is added to the flue gas stream continuously, so as to maintain the NO.sub.x removal efficiency in an amount of at least 70% of an initial NO.sub.x efficiency. E54. The method of embodiment 53 wherein the continuous addition of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 99% of a total flow rate of the upstream NO.sub.x compounds. E55. A method comprising: providing at least one filter medium wherein the at least one filter medium comprises at least one catalyst material; flowing a flue gas stream transverse to a cross-section of the at least one filter medium, such that the flue gas stream passes through the cross section of the at least one filter medium from an upstream side of the filter medium to a downstream side of the filter medium; wherein the flue gas stream comprises: NO.sub.x compounds comprising: Nitric Oxide (NO), and Nitrogen Dioxide (NO.sub.2); Sulfur Dioxide (SO.sub.2); and Ammonia (NH.sub.3); maintaining an NO.sub.x removal efficiency of the at least one filter medium in an amount of at least 70% of an initial NO.sub.x efficiency by: providing an NO.sub.2 concentration, measured from the upstream side of the filter medium, in a range from 2% to 99% of a total concentration of the NO.sub.x compounds; and controlling NO.sub.2 concentration, measured from the downstream side of the filter medium, to a range of from 0.0001% to 0.5% of the concentration of the flue gas stream
wherein the method cleans the flue gas stream. E56. The method of embodiment 55, wherein the NO.sub.x removal efficiency of the at least one filter medium is maintained in a range of 70% to 99% of the initial NO.sub.x efficiency. E57. The method of embodiment 55, 60, or any combination thereof, wherein during the maintaining of the NO.sub.x removal efficiency, the NO.sub.2 concentration is increased periodically. E58. The method of embodiment 57, wherein the periodic increase of NO.sub.2 comprises increasing NO.sub.2 every 1 to 40,000 hours. E59. The method of embodiment 57, 58, or any combination thereof, wherein the periodic increase occurs at constant time intervals. E60. The method of embodiment 57, 58, or any combination thereof, wherein the periodic increase occurs at variable time intervals. E61. The method of embodiment 60, wherein variable time intervals are random time intervals. E62. The method of any of embodiments 55, 60, or any combination thereof, wherein during the providing of the NO.sub.2 concentration, the NO.sub.2 concentration is provided continuously. E63. The method of embodiment 62, wherein the continuous providing of the NO.sub.2 comprises providing NO.sub.2 at a flow rate of 2% to 99% of a total flow rate of the upstream NO.sub.x compounds.

EXAMPLES

Example 1: In-Situ Flow-Through Regeneration of Filter Medium Including a Catalyst Coated Composite Article by NO and NO.SUB.2 .Gas Mixture

(95) An exemplary filter medium including a non-limiting example of a catalyst material in the form of a catalyst coated composite article was prepared on a porous substrate having active catalyst particles adhered to the surface by a polymer adhesive according to U.S. Pat. No. 6,331,351.

(96) In-Situ Flow-Through Regeneration by NO and NO.sub.2 Mixture

(97) The filter medium including the catalyst coated composite sample was returned from the field after exposure to a flue gas stream. The deposition of ammonium bisulfate on the returned sample was confirmed by Fourier-transform infrared spectroscopy (FTIR, Thermal Nicolet iS50). During an in-situ regeneration, a 4.5 inch (1.77 cm)4.5 inch (1.77 cm) sample filter medium including a catalyst coated composite sample was placed in a reactor. A gas mixture including 310 ppm NO, 330 ppm NO.sub.2, 4% O.sub.2, 8% water moisture and N.sub.2 was set to flow-through the catalyst coated composite sample at 230 C. with a total flowrate of 2 L/min. The gas phase NO and NO.sub.2 concentration were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). The NO and NO.sub.2 gas mixture was obtained by partially oxidizing NO to NO.sub.2 by O.sub.3 generated from the TG-20 O.sub.3 generator (Ozone solutions, Hull, Iowa). NO.sub.x removal efficiency was measured before in-situ regeneration treatment and 2, 4, 6, 8, 10 hours after in-situ regeneration treatment.

(98) NO.sub.x Reaction Efficiency

(99) The filter medium including the catalyst coated composite article was tested for catalytic NO.sub.x removal efficiency from a simulated flue gas at 230 C. The simulated flue gas contained 200 ppm NO, 200 ppm NH.sub.3, 5% O.sub.2, and N.sub.2 with a total flowrate of 3.4 L/min. To determine NO.sub.x removal efficiency, the upstream (i.e., the concentration of NO.sub.x entering into the chamber before exposure to the filter medium) and downstream concentration (i.e. the concentration of NO.sub.x exiting the chamber after exposure to the filter medium) of NO were monitored with a MKS MULTI-GAS' 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). NO.sub.x removal efficiency was calculated according to the following formula where NO indicates the concentration of NO in the respective stream.

(100) NO.sub.x removal efficiency (DeNO.sub.x) (%)=(NO inNO out)/NO in100%. Results are shown in FIG. 2.

Example 2: In-Situ Flow-Through Regeneration of Filter Medium Including a Catalytic Composite Article by NO and NO.SUB.2 .Gas Mixture

(101) A filter medium including a catalytic composite article is formed according to International Publication No. WO 2019/099025. The filter medium included a catalytic composite article having a layered assembly that included a polytetrafluoroethylene (PTFE)+catalyst composite membrane having a first, upstream side and a second, downstream side; and one or more felt batts. Each felt batt was formed of fleece formed from PTFE staple fiber. The filter medium was connected together by a plurality of perforations formed by a needle punching process, by a needling process, or both.

(102) The PTFE+catalyst composite membrane of the filter medium described above were prepared using the general dry blending methodology taught in U.S. Pat. No. 7,791,861. to form composite tapes that were then uniaxially expanded according to the teachings of U.S. Pat. No. 3,953,556. The resulting porous fibrillated expanded PTFE (ePTFE) composite membranes included supported catalyst particles durably enmeshed and immobilized with the ePTFE node and fibril matrix.

(103) In-Situ Flow-Through Regeneration by NO and NO.sub.2 Mixture

(104) The sample filter medium including the sample catalytic composite article described above was in-situ fouled by 400 ppm NO, 440 ppm NH.sub.3, 3000 ppm SO.sub.2 and 8% water moisture at 230 C. and returned from Innovative combustion Technologies (ICT). During an in-situ regeneration, a particular filter medium including a square catalytic composite sample (4.5 inch4.5 inch) returned from ICT was placed in a reactor. A gas mixture including 330 ppm NO, 330 ppm NO.sub.2, 4% O.sub.2, 8% water moisture, and N.sub.2 was set to flow-through the catalytic composite sample at 230 C. with a total flowrate of 2 L/min. The NO and NO.sub.2 gas mixture was obtained by partially oxidizing NO to NO.sub.2 by O.sub.3 generated from the TG-20 O.sub.3 generator (Ozone solutions, Hull, Iowa). NO.sub.x removal efficiency was measured before in-situ regeneration treatment and 4, 10, 15, 21, 24 hours after in-situ regeneration treatment. The downstream (i.e. the concentration of NO.sub.x exiting the chamber after exposure to the filter medium) gas phase NO and NO.sub.2 concentrations were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.).

(105) NO.sub.x Reaction Efficiency

(106) The filter medium including the sample catalytic composite article was tested for catalytic NO.sub.x removal efficiency at 230 C. from a simulated flue gas. The simulated flue gas contained 200 ppm NO, 200 ppm NH.sub.3, 5 vol % O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. In order to determine NO.sub.x removal efficiency, the upstream (i.e., the concentration of NO.sub.x entering into the chamber before exposure to the filter medium) and downstream concentration (i.e. the concentration of NO.sub.x exiting the chamber relative after exposure to the filter medium) of NO were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). NO.sub.x removal efficiency was calculated according to the following formula where NO indicates the concentration of NO in the respective stream.

(107) NO.sub.x removal efficiency (DeNO.sub.x) (%)=(NO inNO out)/NO in100%

(108) Relative DeNO.sub.x removal efficiency (%)=DeNO.sub.x after regeneration/DeNO.sub.x of a fresh control sample. Results are shown in FIGS. 3 and 4.

Example 3: In-Situ Flow-Through Regeneration of Filter Medium Including a Catalytic Composite Article by NO, NO.SUB.2 .and NH.SUB.3 .Gas Mixture

(109) A catalytic composite article was used as described in Example 2.

(110) In-Situ Flow-Through Regeneration by NO, NO.sub.2, and NH.sub.3 Mixture

(111) Sample filter medium including the sample catalytic composite article described in Example 2 in-situ fouled by 400 ppm NO, 440 ppm NH.sub.3, 3000 ppm SO.sub.2 and 8% water moisture at 230 C. and returned from Innovative combustion Technologies (ICT). During an in-situ regeneration, a particular filter medium including a square catalytic composite sample (4.5 inch4.5 inch) returned from ICT was placed in a reactor. A gas mixture including 330 ppm NO, 330 ppm NO.sub.2, 85 ppm NH.sub.3, 4% O.sub.2, 8% water moisture, and N.sub.2 was set to flow-through the catalytic composite sample at 230 C. with a total flowrate of 2 L/min. The NO+NO.sub.2 gas mixture was obtained by partially oxidizing NO to NO.sub.2 by O.sub.3 generated from the TG-20 O.sub.3 generator (Ozone solutions, Hull, Iowa). NO.sub.x removal efficiency was measured before in-situ regeneration treatment and 4, 10, 15, 21 hours after in-situ regeneration treatment. The downstream (i.e. the concentration of NO.sub.x exiting the chamber after exposure to the filter medium) gas phase NO and NO.sub.2 concentrations were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.).

(112) NO.sub.x Reaction Efficiency

(113) The filter medium including the sample catalytic composite article was tested for catalytic NO.sub.x removal efficiency at 230 C. from a simulated flue gas as described in Example 2.

(114) NO.sub.x removal efficiency (DeNO.sub.x) (%)=(NO inNO out)/NO in100%

(115) Relative DeNO.sub.x removal efficiency (%)=DeNO.sub.x after regeneration/DeNO.sub.x of a fresh control sample. Results are shown in FIGS. 5 and 6.

Example 4: In-Situ Flow-By Regeneration of Filter Medium Including a Catalytic Composite Article by NO, NO.SUB.2 .and NH.SUB.3 .Gas Mixture

(116) A catalytic composite article as described in Example 2 was used.

(117) In-Situ Flow-By Regeneration by NO, NO.sub.2, and NH.sub.3 Mixture

(118) A sample filter medium including the sample catalytic composite article described in Example 2 in-situ fouled by 400 ppm NO, 440 ppm NH.sub.3, 3000 ppm SO.sub.2 and 8% water moisture at 230 C. and returned from Innovative combustion Technologies (ICT). During an in-situ regeneration, a particular filter medium including a square catalytic composite sample (4.5 inch4.5 inch) returned from ICT was wrapped around a hollow elliptic cylinder stainless steel mesh and placed in a reactor. A gas mixture including 330 ppm NO, 330 ppm NO.sub.2, 85 ppm NH.sub.3, 4% O.sub.2, 8% water moisture, and N.sub.2 was set to flow-by the catalytic composite sample at 230 C. with a total flowrate of 2 L/min. The NO+NO.sub.2 gas mixture was obtained by partially oxidizing NO to NO.sub.2 by O.sub.3 generated from the TG-20 O.sub.3 generator (Ozone solutions, Hull, Iowa). NO.sub.x removal efficiency was measured before in-situ regeneration treatment and 4 hours after in-situ regeneration treatment.

(119) NO.sub.x Reaction Efficiency

(120) The filter medium including the sample catalytic composite article was tested for catalytic NO.sub.x removal efficiency at 230 C. from a simulated flue gas as described in Example 2.

(121) NO.sub.x removal efficiency (DeNO.sub.x) (%)=(NO inNO out)/NO in100%

(122) Relative DeNO.sub.x removal efficiency (%)=DeNO.sub.x after regeneration/DeNO.sub.x of a fresh control sample. Results are shown in FIG. 7.

Example 5: In-Situ Flow-Through Regeneration of Filter Medium Including Catalytic Filter Bags by NO, NO.SUB.2 .and NH.SUB.3 .Gas Mixture

(123) Four catalytic filter bags (65 mm in diameter, 1630 mm in length) were prepared from the catalytic composite articles described in Example 2.

(124) In-Situ Deposition of Ammonium Bisulfate

(125) The filter medium including the sample catalytic filter bags were in-situ fouled at Innovative combustion Technologies by 200 ppm NO, 240 ppm NH.sub.3, 3000 ppm SO.sub.2 and 8% water moisture at 230 C. for 4 hours.

(126) In-Situ Flow-Through Regeneration by NO, NO.sub.2, and NH.sub.3 Mixture

(127) During an in-situ regeneration, a particular filter medium including 4 catalytic filter bags in-situ fouled as described above were used. A gas mixture including 30 ppm NO, 30 ppm NO.sub.2, 8 ppm NH.sub.3, 10% O.sub.2, 8% water moisture, and N.sub.2 was set to flow-through the catalytic filter bags at 230 C. with a total flowrate of 25.3 SCFM for 20 hours.

(128) NO.sub.x Reaction Efficiency

(129) The filter medium including the sample catalytic filter bags were tested for NO.sub.x removal efficiency at Innovative Combustion Technologies from a simulated flue gas at 230 C. The simulated flue gas contained 200 ppm NO, 190 ppm NH.sub.3, 10% O.sub.2, 8% water moisture, and N.sub.2 with a total flowrate of 25.3 standard cubic feet per minute (SCFM). In order to determine NO.sub.x removal efficiency, the upstream (i.e., the concentration of NO.sub.x entering into the chamber before exposure to the filter medium) and downstream concentration (i.e. the concentration of NO.sub.x exiting the chamber relative after exposure to the filter medium) of NO and NO.sub.2 were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). NO.sub.x removal efficiency was calculated according to the following formula where NO.sub.x indicates the total concentration of NO and NO.sub.2 in the respective stream.

(130) NO.sub.x removal efficiency (DeNO.sub.x efficiency) (%)=(NO.sub.x inNO.sub.x out)/NO.sub.x in100%. Results are shown in FIG. 8.

Example 6: Long Term NO.SUB.x .Removal Reaction with Exposure to SO.SUB.2

(131) A catalytic composite article as described in Example 2 was used.

(132) Long Term Flow-Through DeNO.sub.x Reaction by NO, NO.sub.2, and NH.sub.3 Mixture (with and without Excess NO.sub.2 in the Downstream Side of the Filter Medium)

(133) The filter medium including the sample catalytic composite article was tested for catalytic NO.sub.x removal efficiency from a simulated flue gas at 230 C. The simulated flue gas included 13.5 ppm SO.sub.2, 200 ppm NO.sub.x (NO+NO.sub.2), 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. The NO.sub.2 was introduced from a gas cylinder. The inlet NO.sub.2 concentration was controlled to have excess NO.sub.2 (1-8 pm) and no excess NO.sub.2 in the downstream (i.e. the concentration of NO.sub.x exiting the chamber after exposure to the filter medium). In order to determine NO.sub.x removal efficiency, the upstream (i.e., the concentration of NO.sub.x entering into the chamber before exposure to the filter medium) and downstream concentration of NO and NO.sub.2 were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). NO.sub.x removal efficiency was calculated according to the following formula where NO.sub.x indicates the total concentration of NO and NO.sub.2 in the respective stream.

(134) NO.sub.x removal efficiency (DeNO.sub.x efficiency) (%)=(NO.sub.x inNO.sub.x out)/NO.sub.x in100%. Results are shown in FIGS. 9-11.

Example 7: In-Situ Flow-Through Regeneration of Filter Medium Including a Catalytic Composite Article by NO, NO.SUB.2 .and NH.SUB.3 .Gas Mixture with Exposure to SO.SUB.2

(135) A catalytic composite article was used as described in Example 2.

(136) In-Situ Flow-Through Regeneration by NO, NO.sub.2, and NH.sub.3 Mixture with Exposure to SO.sub.2 (with Controlled NO.sub.2 Slip in the Downstream Side of the Filter Medium)

(137) Sample filter medium including the sample catalytic composite article described in Example 2 was in-situ fouled by 400 ppm NO, 440 ppm NH.sub.3, 3000 ppm SO.sub.2 and 8% water moisture at 230 C. and returned from Innovative combustion Technologies (ICT). During an in-situ regeneration, a particular filter medium including a square catalytic composite sample (4.5 inch4.5 inch) returned from ICT was placed in a reactor. Catalytic NO.sub.x removal efficiency before regeneration (in the period of 0-2 hours), during regeneration (in the period of 3-51 hours) and after regeneration (in the period of 55-60 hours) were shown in FIG. 12. Catalytic NO.sub.x removal efficiency before and after regeneration were tested at 230 C. with 200 ppm NO, 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. During the regeneration, the simulated flue gas included 13.5 ppm SO.sub.2, 200 ppm NO.sub.x (NO+NO.sub.2), 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. The inlet NO.sub.2 concentration was controlled to have excess NO.sub.2 (1-5 ppm, FIG. 12) slip in the downstream (i.e. the concentration of NO.sub.x exiting the chamber after exposure to the filter medium). The NO.sub.2 was introduced from a gas cylinder.

(138) In order to determine NO.sub.x removal efficiency, the upstream (i.e., the concentration of NO.sub.x entering into the chamber before exposure to the filter medium) and downstream concentration of NO and NO.sub.2 were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). NO.sub.x removal efficiency was calculated according to the following formula where NO.sub.x: indicates the total concentration of NO and NO.sub.2 in the respective stream.

(139) NO.sub.x removal efficiency (DeNO.sub.x efficiency) (%)=(NO.sub.x inNO.sub.x out)/NO.sub.x in100%. Results are shown in FIG. 12.

Example 8: In-Situ Flow-Through Regeneration of Filter Medium Including a Catalytic Composite Article by NO, NO.SUB.2 .and NH.SUB.3 .Gas Mixture with Exposure to SO.SUB.2

(140) A catalytic composite article was used as described in Example 2.

(141) In-Situ Flow-Through Regeneration by NO, NO.sub.2, and NH.sub.3 Mixture with Exposure to SO.sub.2 (with Controlled NO.sub.2 Slip in the Downstream Side of the Filter Medium)

(142) Sample filter medium including the sample catalytic composite article described in Example 2 was in-situ fouled by 400 ppm NO, 440 ppm NH.sub.3, 3000 ppm SO.sub.2 and 8% water moisture at 230 C. and returned from Innovative combustion Technologies (ICT). During an in-situ regeneration, a particular filter medium including a square catalytic composite sample (4.5 inch4.5 inch) returned from ICT was placed in a reactor. Before the in-situ regeneration, catalytic NO.sub.x removal efficiency (FIG. 13) was tested at 230 C. with 200 ppm NO, 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. After checking the NO.sub.x removal efficiency before regeneration, a 6.2 days (148 hours) in-situ flow-through regeneration was conducted. During the regeneration, the simulated flue gas included 13.5 ppm SO.sub.2, 200 ppm NO.sub.x (NO+NO.sub.2), 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. The inlet NO.sub.2 concentration was controlled to have excess NO.sub.2 (1-12 ppm) slip in the downstream (i.e. the concentration of NO.sub.x exiting the chamber after exposure to the filter medium). The NO.sub.2 was introduced from a gas cylinder. Catalytic NO.sub.x removal efficiency during the in-situ regeneration was shown in FIG. 13. After the in-situ regeneration, catalytic NO.sub.x removal efficiency was tested at 230 C. with 200 ppm NO, 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min, shown in FIG. 13.

(143) To determine NO.sub.x removal efficiency, the upstream (i.e., the concentration of NO.sub.x entering into the chamber before exposure to the filter medium) and downstream concentration of NO and NO.sub.2 were monitored with a MKS MULTI-GAS 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). NO.sub.x removal efficiency was calculated according to the following formula where NO.sub.x indicates the total concentration of NO and NO.sub.2 in the respective stream.

(144) NO.sub.x removal efficiency (DeNO.sub.x efficiency) (%)=(NO.sub.x inNO.sub.x out)/NO.sub.x in100%. Results are shown in FIG. 13.

Example 9: Long Term NO.SUB.x .Removal Reaction with Exposure to SO.SUB.2 .with Periodic in-Situ Flow-Through Regeneration of Filter Medium

(145) A catalytic composite article was used as described in Example 2.

(146) Periodic In-Situ Flow-Through Regeneration by NO, NO.sub.2, and NH.sub.3 Mixture with Exposure to SO.sub.2 (with Controlled NO.sub.2 Slip in the Downstream Side of the Filter Medium)

(147) The filter medium including the sample catalytic composite article described in Example 2 was tested for catalytic NO.sub.x removal efficiency from a simulated flue gas at 230 C. for over 400 hours (16.7 days). The simulated flue gas included 13.5 ppm SO.sub.2, 200 ppm NO, 200 ppm NH.sub.3, 5% O.sub.2, 5% water moisture, and N.sub.2 with a total flowrate of 3.4 L/min. The DeNO.sub.x removal efficiency change with time was shown in FIG. 10 and used as raw data (Tested DeNO.sub.x in FIG. 14) to extrapolate the long term DeNO.sub.x removal efficiency (Simulated DeNO.sub.x in FIG. 14) change with operation time. In-situ flow-through regeneration by NO, NO.sub.2, and NH.sub.3 mixture (with controlled NO.sub.2 slip in the downstream side of the filter medium) will be started once the DeNO.sub.x removal efficiency decreased to 72%, or 78% of the initial DeNO.sub.x removal efficiency (initial DeNO.sub.x removal efficiency was 92%, FIG. 14). According to Example 8, after 148 hours (6.2 days) in-situ flow-through regeneration by NO, NO.sub.2, and NH.sub.3 mixture (with controlled NO.sub.2 slip in the downstream side of the filter medium), the DeNO.sub.x removal efficiency can be recovered to 83%, or 90% of the initial DeNO.sub.x removal efficiency (FIG. 14). After the first regeneration, periodic in-situ flow-through regeneration can be conducted periodically once the DeNO.sub.x removal efficiency decreased to 72% or 78% of the initial DeNO.sub.x removal efficiency. This process is illustrated in FIG. 14.

(148) Variations, modifications and alterations to embodiments of the present disclosure described above will make themselves apparent to those skilled in the art. All such variations, modifications, alterations and the like are intended to fall within the spirit and scope of the present disclosure, limited solely by the appended claims.

(149) While several embodiments of the present disclosure have been described, it is understood that these embodiments are illustrative only, and not restrictive, and that many modifications may become apparent to those of ordinary skill in the art. For example, all dimensions discussed herein are provided as examples only, and are intended to be illustrative and not restrictive.

(150) Any feature or element that is positively identified in this description may also be specifically excluded as a feature or element of an embodiment of the present as defined in the claims.

(151) The disclosure described herein may be practiced in the absence of any element or elements, limitation or limitations, which is not specifically disclosed herein. Thus, for example, in each instance herein, any of the terms comprising, consisting essentially of and consisting of may be replaced with either of the other two terms. The terms and expressions which have been employed are used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the disclosure.