Method for regenerating filter medium and cleaning flue gas

Abstract

To provide a method for regenerating a filter medium and cleaning flue gas.SOLUTION: Some non-limiting embodiments of the present disclosure relate to a method for regenerating at least one filter medium, and the method includes flowing of a flue gas stream through at least one filter medium or near the at least one filter medium at a first temperature, and increasing the temperature of the flue gas from the first temperature to a second temperature exceeding the first temperature. Some non-limiting embodiments of the present disclosure relate to a method of cleaning a flue gas stream, the method comprising maintaining NOx removal efficiency by increasing the temperature of the flue gas stream from the first temperature to the second temperature exceeding the first temperature.SELECTED DRAWING: Figure 2

Description

[Technical field]

[0001] The present disclosure generally relates to one or more methods of regenerating at least one filter media and scrubbing a flue gas stream. [Background technology]

[0002] Coal-fired power plants, municipal waste incinerators, and oil refineries emit significant amounts and types of environmental pollutants, including nitrogen oxides (NO x Burning coal produces large amounts of flue gases that contain sulfur dioxide (SO2) compounds, mercury (Hg) vapor, and particulate matter (PM). In the United States, burning coal alone produces about 27 million tons of SO2 and 45 tons of Hg each year. Summary of the Invention

[0003] NO from industrial flue gases, such as those from coal-fired power plants x There is a need for improved methods for removing compounds, sulfur oxides, mercury vapor and particulate matter.

[0004] Some embodiments of the present disclosure relate to a method of regenerating at least one filter medium, the method comprising providing at least one filter medium, the at least one filter medium comprising at least one catalytic material and ammonium bisulfate (ABS), ammonium sulfate (AS), or any combination thereof; flowing a flue gas stream through or adjacent the at least one filter medium, the flue gas stream comprising NO, including nitric oxide (NO) and nitrogen dioxide (NO2), x and the flue gas stream is at a first temperature during the flow process. x increasing the NO removal efficiency of the at least one filter medium; x Increasing the removal efficiency includes adding ammonia (NH3) at a concentration in the range of 0.0001% to 0.5% of a concentration of the flue gas stream, and increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature.

[0005] Some embodiments of the present disclosure relate to a method of scrubbing a flue gas stream, the method comprising: providing at least one filter medium, wherein the at least one filter medium comprises at least one catalytic material; flowing a flue gas stream across 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 from an upstream side to a downstream side of the filter medium; wherein the flue gas stream is scrubbed with NO, including nitric oxide (NO) and nitrogen dioxide (NO2). x The flue gas stream is at a first temperature during a flow process, and the at least one filter medium has a constant NO 2 concentration. x maintaining a constant NO removal efficiency of said at least one filter medium; x Maintaining the removal efficiency includes increasing the temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature.

[0006] Some embodiments of the present disclosure relate to a method of scrubbing a flue gas stream, the method comprising: flowing the flue gas stream adjacent a cross-section of at least one filter medium such that the flue gas stream flows 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 is a mixture of NO, including nitric oxide (NO) and nitrogen dioxide (NO2). x The at least one filter medium contains a mixture of sulfur dioxide (SO2), sulfur dioxide (SO2), and ammonia (NH3), wherein the flue gas stream is at a first temperature during a flow process. x maintaining a constant NO removal efficiency of said at least one filter medium; x Maintaining the removal efficiency includes increasing the temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature.

[0007] Some embodiments of the present disclosure relate to a method of scrubbing a flue gas stream, the method comprising: flowing the flue gas stream across a cross-section of at least one filter medium such that the flue gas stream passes through 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 is scrubbed with NO, including nitric oxide (NO) and nitrogen dioxide (NO2). x and ammonia (NH), wherein the flue gas stream is at a first temperature during a flow process. The method comprises: increasing the temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature to produce an initial NO2 gas mixture; x The at least one filter medium is at least 70% efficient. x This includes maintaining removal efficiency.

[0008] In some embodiments, the second temperature is at least 10° C. higher than the first temperature.

[0009] In some embodiments, the second temperature is 10° C. to 100° C. higher than the first temperature.

[0010] In some embodiments, the first temperature is in the range of 180°C to 230°C.

[0011] In some embodiments, the second temperature is at least 240°C.

[0012] In some embodiments, the second temperature is up to 280°C.

[0013] In some embodiments, the second temperature is in the range of 240°C to 280°C.

[0014] In some embodiments, the second temperature is in the range of 240°C to 260°C.

[0015] In some embodiments, the concentration of SO2 in the flue gas stream does not exceed 1000 ppm during the maintaining step.

[0016] In some embodiments, the concentration of SO2 in the flue gas stream does not exceed 10 ppm during the maintaining step. [Brief description of the drawings]

[0017] Some embodiments of the present disclosure are described herein, by way of example only, with reference to the accompanying drawings. With particular reference now to the drawings in detail, it is emphasized that the illustrated embodiments are intended by way of example and for illustrative discussion of embodiments of the present disclosure. In this regard, the description with the drawings will make apparent to those skilled in the art how embodiments of the present disclosure may be practiced.

[0018] [Figure 1A] FIG. 1A illustrates an exemplary filter media embodiment according to the present disclosure. [Figure 1B] FIG. 1B illustrates an exemplary filter media embodiment according to the present disclosure. [Figure 1C] FIG. 1C illustrates an exemplary filter media embodiment according to the present disclosure. [Figure 1D] FIG. 1D illustrates an exemplary filter media embodiment according to the present disclosure.

[0019] [Diagram 2] FIG. 2 shows exemplary NOx removal efficiencies of a filter media described herein before ammonium bisulfate loading, after ammonium bisulfate loading, and after thermal regeneration.

[0020] [Diagram 3] FIG. 3 shows the comparative NOx removal efficiency of the filter media described herein before ammonium bisulfate loading, after ammonium bisulfate loading, and after thermal regeneration.

[0021] [Figure 4] FIG. 4 shows further exemplary NOx removal efficiencies of filter media described herein before ammonium bisulfate loading, after ammonium bisulfate loading, and after thermal regeneration.

[0022] [Diagram 5]FIG. 5 shows exemplary NOx removal efficiencies for catalyzed filter samples after ammonium bisulfate loading and thermal regeneration as described herein. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0023] Among the disclosed benefits and improvements, other objects and advantages of the present disclosure will become apparent from the following description taken in conjunction with the accompanying drawings. Detailed embodiments of the present disclosure are disclosed herein. However, it should be understood that the disclosed embodiments are merely exemplary of the disclosure, which may be embodied in various forms. Moreover, each of the examples provided with respect to the various embodiments of the present disclosure are intended to be illustrative and not limiting.

[0024] Throughout the specification and claims, the following terms shall take the meanings expressly associated therewith, unless the context clearly dictates otherwise. As used herein, the phrases "in one embodiment," "in an embodiment," and "in some embodiments" do not necessarily refer to the same embodiment, although they may. Additionally, as used herein, the phrases "in another embodiment" and "in some other embodiments" do not necessarily refer to different embodiments, although they may. It is intended that all embodiments of the present disclosure can be combined without departing from the scope or spirit of the present disclosure.

[0025] As used herein, the term "based on" is not exclusive and allows for based on additional unrecited factors unless the context clearly dictates otherwise. Additionally, throughout the specification, the meanings of "a," "an," and "the" include plural references. The meaning of "in" includes "in" and "on."

[0026] As used herein, the term "flow through" means that the flue gas flow flows across the cross-section of at least one filter medium such that the flue gas flow passes through the cross-section of the at least one filter medium. In some embodiments of the "flow through" configuration, the flue gas flow is flowed perpendicular to the cross-section of the at least one filter medium.

[0027] As used herein, the term "flow by" means that the flue gas stream does not flow across the cross-section of the at least one filter media, such that the flue gas does not flow through the cross-section of the filter media. In some embodiments of the "flow by" configuration, the flue gas stream is flowed parallel to the cross-section of the at least one filter media.

[0028] As used herein, "upstream" refers to a location of the flue gas stream before it enters the filter media. In a "flow-through" context, "upstream" can refer to a location of the flue gas stream before it enters the cross-section of the filter media. In a "flow-by" context, "upstream" can refer to a location of the flue gas stream before it enters an enclosure (e.g., a housing, filter bag, or other suitable enclosure described herein) that contains the filter media.

[0029] As used herein, "downstream" refers to the location of the flue gas flow after it exits the filter media. In a "flow-through" context, "downstream" can refer to the location of the flue gas flow after it exits the cross-section of the filter media. In a "flow-by" context, "downstream" can refer to the location of the flue gas flow after it exits the enclosure (e.g., a housing, filter bag, or other suitable enclosure described herein) that contains the filter media.

[0030] As used herein, "NO x The term "compound" refers to any oxide of nitrogen. In some non-limiting embodiments, "NO x"Compounds" may specifically refer to gaseous oxides of nitrogen, which are known environmental pollutants.

[0031] As used herein, the term "catalytic composite article" as illustrated in the examples refers to any material that includes a combination of at least one catalytic material according to any embodiment described herein and at least one additional material. The additional material is not limited to any particular type of material and can 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 can be a porous catalytic film in some non-limiting examples.

[0032] As used herein, the term "NO" as shown in the examples x Removal efficiency ("DeNO x The term "efficiency" (also referred to as "efficiency") refers to a percentage value determined (e.g., calculated) according to the following algorithm: NO x Removal efficiency (DeNO x Efficiency (%) = (NO xin -NO xout ) / NO xin ×100%

[0033] Some embodiments of the present disclosure relate to methods of regenerating at least one filter media.

[0034] In some embodiments, the at least one filter medium comprises at least one catalytic material. In some embodiments, the at least one catalytic material comprises at least one of vanadium monoxide (VO), vanadium trioxide (VO), vanadium dioxide (VO), vanadium pentoxide (VO), tungsten trioxide (WO), molybdenum trioxide (MoO), titanium dioxide (TiO), silicon dioxide (SiO), aluminum trioxide (AlO), manganese oxide (MnO), zeolite, or any combination thereof. In some embodiments, the at least one catalytic material is in the form of catalytic particles.

[0035] In some embodiments, the at least one filter media includes an upstream side and a downstream side. In some embodiments, the at least one filter media is disposed within at least one filter bag. In some embodiments, multiple filter media are disposed within a single filter bag. In some embodiments, the at least one filter bag is contained within at least one filter bag housing. In some embodiments, multiple filter bags are disposed within a single filter bag housing.

[0036] In some embodiments, a filter medium includes a porous guard layer and a porous catalyst layer. In some embodiments, the porous catalyst layer includes at least one catalyst material. In some embodiments, the at least one catalyst material is disposed on the porous catalyst layer. In some embodiments, the at least one catalyst material is within (e.g., embedded in) the porous catalyst layer.

[0037] In some embodiments, the porous protective layer comprises a microporous layer, hi some embodiments, the microporous layer comprises an expanded polytetrafluoroethylene (ePTFE) membrane.

[0038] In some embodiments, the at least one catalytic material is adhered to the filter media by at least one adhesive. In some embodiments, the at least one catalytic material is adhered to the porous catalyst layer by at least one adhesive. In some exemplary embodiments, the at least one filter media is in the form of a filter bag, such that adhesion of the at least one catalytic material to the porous catalyst layer by the at least one adhesive forms a coated filter bag. In some embodiments, the at least one catalytic material is in the form of catalyst particles, such that the coated filter bag is coated with the catalyst particles.

[0039] In some embodiments, the at least one adhesive is selected from polytetrafluoroethylene (PTFE), fluorinated ethylene propylene (FEP), high molecular weight polyethylene (HMWPE), high molecular weight polypropylene (HMWPP), perfluoroalkoxyalkane (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), perfluoroalkoxyalkane (PFA), polyvinylidene fluoride (PVDF), vinylidene fluoride (THV), chlorofluoroethylene (CFE), and any combination thereof.

[0040] In some embodiments, the porous catalyst layer includes at least one polymer substrate. In some embodiments, the at least one polymer substrate is one of polytetrafluoroethylene, poly(ethylene-co-tetrafluoroethylene), ultra-high molecular weight polyethylene, polyparaxylylene, polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, glass fiber, or any combination thereof. In some embodiments, the at least one polymer substrate is selected from the group consisting of polytetrafluoroethylene, poly(ethylene-co-tetrafluoroethylene), ultra-high molecular weight polyethylene, polyparaxylylene, polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, glass fiber, and any combination thereof.

[0041] In some embodiments, the porous catalyst layer comprises at least one ceramic substrate. In some embodiments, the at least one ceramic substrate is in the form of a ceramic candle as described herein. In some embodiments, a ceramic substrate comprises ceramic fibers. In some embodiments, the ceramic fibers comprise an alkali metal silicate, an alkaline earth metal silicate, an aluminosilicate, or any combination thereof.

[0042] In some embodiments, the porous catalyst layer is in the form of a layered assembly including a porous catalyst film and one or more felt pads. In some embodiments, the one or more felt pads are disposed on at least one side of the porous catalyst film. In some embodiments, the porous catalyst film includes at least one catalytic material. In some embodiments, the at least one catalytic material is disposed on the porous catalyst film. In some embodiments, the at least one catalytic material is within (e.g., embedded in) the porous catalyst film.

[0043] In some embodiments, the one or more felt batts comprise at least one of polytetrafluoroethylene (PTFE) felt, PTFE fleece, expanded polytetrafluoroethylene (ePTFE) felt, ePTFE fleece, woven fluoropolymer staple fibers, nonwoven fluoropolymer staple fibers, or any combination thereof.

[0044] In some embodiments, the one or more felt batts are selected from the group consisting of polytetrafluoroethylene (PTFE) felt, PTFE fleece, expanded polytetrafluoroethylene (ePTFE) felt, ePTFE fleece, woven fluoropolymer staple fibers, nonwoven fluoropolymer staple fibers, and any combination thereof.

[0045] In some embodiments, the porous catalyst film comprises a membrane. In some embodiments, the porous catalyst film comprises a polymer membrane. In some embodiments, the porous catalyst film comprises a fluoropolymer membrane, which may also be referred to as a porous catalytic fluoropolymer film. In some embodiments, the porous catalyst film comprises an expanded polytetrafluoroethylene (ePTFE) membrane.

[0046] In some embodiments, the porous catalyst film comprises catalyst particles entangled within the ePTFE membrane. In some embodiments, the ePTFE membrane has a microstructure comprising nodes, fibrils, or any combination thereof. In some embodiments, the catalyst particles may be entangled in the microstructure. In some embodiments, the catalyst particles may be entangled in the nodes. In some embodiments, the catalyst particles may be entangled in the fibrils. In some embodiments, the catalyst particles may be entangled in the nodes and fibrils.

[0047] 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 at least one ceramic material is selected from silica aluminate, calcium magnesium silicate, calcium silicate fibers, or any combination thereof. In some embodiments, the catalyst particles form a coating on the at least one ceramic material.

[0048] In some embodiments, the at least one filter media may include any material configured to capture at least one of solid particulates, liquid aerosols, or any combination thereof from the flue gas stream, hi some embodiments, the at least one filter media is in the form of at least one of a filter bag, a honeycomb, a monolith, or any combination thereof.

[0049] In some embodiments, at least one filter medium comprises an ammonium bisulfate (ABS) deposit, an ammonium sulfate (AS) deposit, or any combination thereof. In some embodiments, the ABS deposit is disposed on at least one catalytic material of the at least one filter medium. In some embodiments, the ABS deposit is disposed within at least one catalytic material of the at least one filter medium.

[0050] In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.1% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 1% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 10% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 25% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 50% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 75% to 99% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 95% to 99% by weight of the at least one filter media during the providing step.

[0051] In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 95% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 75% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 50% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 25% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 10% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 1% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 0.01% to 0.1% by weight of the at least one filter media during the providing step.

[0052] In some embodiments, the ABS deposit is present in a concentration ranging from 0.1% to 95% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 1% to 75% by weight of the at least one filter medium during the providing step. In some embodiments, the ABS deposit is present in a concentration ranging from 10% to 50% by weight of the at least one filter medium during the providing step.

[0053] In some embodiments, a method of regenerating at least one filter medium includes 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 a 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.

[0054] In some embodiments, a method of regenerating at least one filter medium includes flowing a flue gas stream adjacent to 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 a 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.

[0055] In some embodiments, the flue gas stream is NO x In some embodiments, the compound includes NO x The compounds include nitric oxide (NO) and nitrogen dioxide (NO2). In some embodiments, the flue gas stream further comprises at least one of oxygen (O2), water (H2O), nitrogen (N2), carbon monoxide (CO), sulfur dioxide (SO2), sulfur trioxide (SO3), one or more hydrocarbons, or any combination thereof.

[0056] In some embodiments, the method of regenerating at least one filter medium comprises: x This includes increasing the removal efficiency.

[0057] In some embodiments, the flue gas stream is at a first temperature while the flue gas stream is flowing, and the NO of the at least one filter medium is x Increasing the removal efficiency includes increasing the temperature of the flue gas stream from a first temperature to a second temperature greater than the first temperature.

[0058] In some embodiments, the first temperature is in the range of 180°C to 230°C. In some embodiments, the first temperature is in the range of 190°C to 230°C. In some embodiments, the first temperature is in the range of 200°C to 230°C. In some embodiments, the first temperature is in the range of 210°C to 230°C. In some embodiments, the first temperature is in the range of 220°C to 230°C.

[0059] In some embodiments, the first temperature is in the range of 180°C to 220°C. In some embodiments, the first temperature is in the range of 180°C to 210°C. In some embodiments, the first temperature is in the range of 180°C to 200°C. In some embodiments, the first temperature is in the range of 180°C to 190°C.

[0060] In some embodiments, the first temperature is in the range of 190° C. to 220° C. In some embodiments, the first temperature is in the range of 200° C. to 210° C.

[0061] In some embodiments, the second temperature is at least 10° C. higher than the first temperature. In some embodiments, the second temperature is at least 20° C. higher than the first temperature. In some embodiments, the second temperature is at least 30° C. higher than the first temperature. In some embodiments, the second temperature is at least 40° C. higher than the first temperature. In some embodiments, the second temperature is at least 50° C. higher than the first temperature. In some embodiments, the second temperature is at least 60° C. higher than the first temperature. In some embodiments, the second temperature is at least 70° C. higher than the first temperature. In some embodiments, the second temperature is at least 80° C. higher than the first temperature. In some embodiments, the second temperature is at least 90° C. higher than the first temperature. In some embodiments, the second temperature is at least 100° C. higher than the first temperature.

[0062] In some embodiments, the second temperature is 10° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 20° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 30° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 40° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 50° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 60° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 70° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 80° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 90° C. to 100° C. higher than the first temperature.

[0063] In some embodiments, the second temperature is 10° C. to 90° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 80° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 70° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 60° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 50° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 40° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 30° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 20° C. higher than the first temperature.

[0064] In some embodiments, the second temperature is 20° C. to 90° C. higher than the first temperature. In some embodiments, the second temperature is 30° C. to 80° C. higher than the first temperature. In some embodiments, the second temperature is 40° C. to 70° C. higher than the first temperature. In some embodiments, the second temperature is 50° C. to 60° C. higher than the first temperature.

[0065] In some embodiments, the second temperature is at least 240°C. In some embodiments, the second temperature is at least 245°C. In some embodiments, the second temperature is at least 250°C. In some embodiments, the second temperature is at least 255°C. In some embodiments, the second temperature is at least 260°C. In some embodiments, the second temperature is at least 265°C. In some embodiments, the second temperature is at least 270°C. In some embodiments, the second temperature is at least 275°C. In some embodiments, the second temperature is at least 280°C.

[0066] In some embodiments, the second temperature is at most 280°C. In some embodiments, the second temperature is at most 275°C. In some embodiments, the second temperature is at most 270°C. In some embodiments, the second temperature is at most 265°C. In some embodiments, the second temperature is at most 260°C. In some embodiments, the second temperature is at most 255°C. In some embodiments, the second temperature is at most 250°C. In some embodiments, the second temperature is at most 245°C. In some embodiments, the second temperature is at most 240°C.

[0067] In some embodiments, the second temperature is in the range of 240°C to 280°C. In some embodiments, the second temperature is in the range of 240°C to 275°C. In some embodiments, the second temperature is in the range of 240°C to 270°C. In some embodiments, the second temperature is in the range of 240°C to 265°C. In some embodiments, the second temperature is in the range of 240°C to 260°C. In some embodiments, the second temperature is in the range of 240°C to 255°C. In some embodiments, the second temperature is in the range of 240°C to 250°C. In some embodiments, the second temperature is in the range of 240°C to 245°C.

[0068] In some embodiments, the second temperature is in the range of 240°C to 275°C. In some embodiments, the second temperature is in the range of 240°C to 270°C. In some embodiments, the second temperature is in the range of 240°C to 265°C. In some embodiments, the second temperature is in the range of 240°C to 260°C. In some embodiments, the second temperature is in the range of 240°C to 255°C. In some embodiments, the second temperature is in the range of 240°C to 250°C. In some embodiments, the second temperature is in the range of 240°C to 245°C.

[0069] In some embodiments, the second temperature is in the range of 245° C. to 275° C. In some embodiments, the second temperature is in the range of 250° C. to 270° C. In some embodiments, the second temperature is in the range of 255° C. to 265° C.

[0070] In some embodiments, the first temperature is raised to the second temperature for 0.25 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 0.5 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 1 hour to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 2 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 5 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 10 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 12 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 24 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 36 hours to 48 hours.

[0071] In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 36 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 24 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 12 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 10 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 5 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 2 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 1 hour. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 0.5 hours.

[0072] In some embodiments, the first temperature is raised to the second temperature for between 0.5 hours and 36 hours. In some embodiments, the first temperature is raised to the second temperature for between 1 hour and 24 hours. In some embodiments, the first temperature is raised to the second temperature for between 2 hours and 12 hours. In some embodiments, the first temperature is raised to the second temperature for between 5 hours and 10 hours.

[0073] In some embodiments, the NO of at least one filter medium x Increasing the removal efficiency further includes adding ammonia (NH3) at a concentration in the range of 0.0001% to 0.5% of the concentration in the flue gas stream. In some embodiments, the NO removal efficiency of the at least one filter medium is x Increasing the removal efficiency further comprises adding NH3 at a concentration in the range of 0.001% to 0.5% of the concentration in the flue gas stream. In some embodiments, the NO removal efficiency of the at least one filter medium is x Increasing the removal efficiency further includes adding ammonia NH3 at a concentration in the range of 0.01% to 0.5% of the concentration of the flue gas stream. In some embodiments, the NO removal efficiency of the at least one filter medium is xIncreasing the removal efficiency further includes adding ammonia NH3 at a concentration in the range of 0.1% to 0.5% of the concentration in the flue gas stream.

[0074] In some embodiments, the NO of at least one filter medium x Increasing the removal efficiency further comprises adding NH3 at a concentration in the range of 0.0001% to 0.1% of the concentration of the flue gas stream. In some embodiments, the NO removal efficiency of the at least one filter medium is x Increasing the removal efficiency further includes adding NH3 at a concentration in the range of 0.0001% to 0.05% of the concentration of the flue gas stream. In some embodiments, the NO removal efficiency of the at least one filter medium is x Increasing the removal efficiency further includes adding NH3 at a concentration in the range of 0.0001% to 0.005% of the concentration in the flue gas stream.

[0075] In some embodiments, the NO of at least one filter medium x Increasing the removal efficiency further comprises adding NH3 at a concentration in the range of 0.005% to 0.1% of the concentration in the flue gas stream. In some embodiments, the NO removal efficiency of the at least one filter medium is x Increasing the removal efficiency further includes adding NH3 at a concentration in the range of 0.005% to 0.05% of the concentration in the flue gas stream.

[0076] In some embodiments, NH is converted to NO in the flue gas stream while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x The NH3 is added in a concentration ratio of 1:100 to 5:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3. xIn some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3. x The NH3 is added in a concentration ratio of 1:2 to 5:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x Compounds are added at concentration ratios ranging from 1:1 to 5:1 based on their concentration.

[0077] In some embodiments, NH is converted to NO in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x The NH3 is added in a concentration ratio of 1:100 to 2:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3.x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x The compounds are added at a concentration ratio of 1:100 to 1:50 based on their concentration.

[0078] In some embodiments, NH is converted to NO in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x Compounds are added at a concentration ratio of 1:10 to 1:2 based on their concentration.

[0079] In some embodiments, even if NH3 is not present in the flue gas stream, NO x The removal efficiency is improved. In some embodiments, the first temperature is increased to the second temperature without adding NH3 to the flue gas stream.

[0080] In some embodiments, the NO of at least one filter medium x The removal efficiency is at least 0.5% higher after the raising step than during the providing step. In some embodiments, the NO 2 removal efficiency of at least one filter medium is at least 0.5% higher after the raising step than during the providing step. x The removal efficiency is at least 1% higher after the raising step than during the providing step. In some embodiments, the NO 2 removal efficiency of at least one filter medium is at least 1% higher after the raising step than during the providing step. x The removal efficiency is at least 5% higher after the raising step than during the providing step. In some embodiments, the NO removal efficiency of at least one filter medium is at least 5% higher after the raising step than during the providing step. xThe removal efficiency is at least 10% higher after the raising step than during the providing step. In some embodiments, the NO 2 removal efficiency of at least one filter medium is at least 10% higher after the raising step than during the providing step. x The removal efficiency is at least 25% higher after the raising step than during the providing step. In some embodiments, the NO 2 removal efficiency of at least one filter medium is at least 25% higher after the raising step than during the providing step. x The removal efficiency is at least 50% higher after the raising step than during the providing step. In some embodiments, the NO 2 removal efficiency of at least one filter medium is at least 50% higher after the raising step than during the providing step. x The removal efficiency is at least 75% higher after the raising step than during the providing step. In some embodiments, the NO 2 removal efficiency of at least one filter medium is at least 75% higher after the raising step than during the providing step. x The removal efficiency is at least 100% higher after the raising step than during the providing step.

[0081] In some embodiments, NO x Increasing the removal efficiency includes removing at least a portion of the ABS deposits, the AS deposits, or any combination thereof, from at least one filter medium. In some embodiments, NO x Increasing the removal efficiency includes removing at least 10% of the ABS deposits, the AS deposits, or any combination thereof, from at least one filter medium. In some embodiments, NO x Increasing the removal efficiency includes removing at least 25% of the ABS deposits, the AS deposits, or any combination thereof, from at least one filter medium. In some embodiments, NO x Increasing the removal efficiency includes removing at least 50% of the ABS deposits, the AS deposits, or any combination thereof, from at least one filter medium. In some embodiments, NO x Increasing the removal efficiency includes removing at least 75% of the ABS deposits, the AS deposits, or any combination thereof from at least one filter medium. In some embodiments, NO x Increasing the removal efficiency includes removing at least 95% of the ABS deposits, the AS deposits, or any combination thereof, from at least one filter medium. In some embodiments, NO xIncreasing the removal efficiency can include removing all of the ABS deposits, the AS deposits, or any combination thereof from at least one filter medium.

[0082] In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 98% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 90% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 50% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 20% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 10% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 5% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 1% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 0.1% by weight of the at least one filter medium.

[0083] In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.1% to 98% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 1% to 98% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 5% to 98% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 10% to 98% by weight of the at least one filter medium. In some embodiments, after the rising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 20% to 98% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 50% to 98% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 90% to 98% by weight of the at least one filter medium.

[0084] In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.1% to 90% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 1% to 50% by weight of the at least one filter medium. In some embodiments, after the raising step, the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 5% to 20% by weight of the at least one filter medium.

[0085] In some embodiments, the concentration of SO2 in the flue gas stream is determined by the NO2 concentration in at least one filter medium. xDuring the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 1000 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream is not more than 500 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 250 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 100 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 75 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream is not more than 50 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 25 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 12 ppm. x During the step of increasing the removal efficiency, the concentration of SO2 in the flue gas stream is not more than 10 ppm. x In some embodiments, the concentration of SO2 in the flue gas stream is increased by increasing the NO2 removal efficiency of at least one filter medium. x In some embodiments, the concentration of SO2 in the flue gas stream is increased by increasing the NO2 removal efficiency of at least one filter medium. x During the process of increasing the removal efficiency, the removal efficiency will not exceed 1 ppm.

[0086] Some embodiments of the present disclosure relate to methods of scrubbing a flue gas stream. In some embodiments, the method of scrubbing a flue gas stream can include flowing the flue gas stream through a filter medium as described herein (i.e., transverse to a cross-section of the filter medium such that the flue gas stream passes through at least one cross-section of the filter medium).

[0087] In some embodiments of the method for scrubbing a flue gas stream, the flue gas stream is scrubbed with NO x In some embodiments, the compound may include NO x The compounds may include nitric oxide (NO) and nitrogen dioxide (NO2). In some embodiments, the flue gas stream may further include sulfur dioxide (SO2) and ammonia (NH3).

[0088] In some embodiments, SO2, NH3, and NO x The compound is at least 1 mg / m based on the total volume of the flue gas stream. 3 In some embodiments, SO2, NH3 and NO x The compound is at least 2 mg / m based on the total volume of the flue gas stream. 3 In some embodiments, SO2, NH3 and NO x The compound is at least 5 mg / m based on the total volume of the flue gas stream. 3 In some embodiments, SO2, NH3 and NO x The compound is at least 10 mg / m based on the total volume of the flue gas stream. 3 In some embodiments, SO2, NH3 and NO x The compound is at least 25 mg / m based on the total volume of the flue gas stream. 3 In some embodiments, SO2, NH3 and NO x The compound is at least 50 mg / m based on the total volume of the flue gas stream. 3 In some embodiments, SO2, NH3 and NO xThe compound is at least 100 mg / m based on the total volume of the flue gas stream. 3 is present in an amount of

[0089] In some embodiments of the method for scrubbing a flue gas stream, the method comprises: x In some embodiments of the method for scrubbing a flue gas stream, the method includes maintaining the NO removal efficiency of at least one filter medium that does not change by more than 1%. x In some embodiments of the method for scrubbing a flue gas stream, the method includes maintaining the NO removal efficiency of at least one filter medium that does not change by more than 5%. x In some embodiments of the method for scrubbing a flue gas stream, the method includes maintaining the NO removal efficiency of at least one filter medium that does not change by more than 10%. x Maintaining the removal efficiency can include:

[0090] In some embodiments, NO x Efficiency is the initial NO x In some embodiments, the NO 2 concentration is maintained at at least 70% of the normal concentration. x Efficiency is the initial NO x In some embodiments, the NO 2 concentration is maintained at at least 75% of the normal concentration. x Efficiency is the initial NO x In some embodiments, the NO 2 concentration is maintained at at least 80% of the efficiency. x Efficiency is the initial NO x In some embodiments, the NO x Efficiency is the initial NO x In some embodiments, the NO 2 concentration is maintained at at least 90% of the efficiency. x Efficiency is the initial NO x In some embodiments, the NO 2 concentration is maintained at at least 95% of the efficiency. x Efficiency is the initial NO x Maintains at least 99% of efficiency.

[0091] In some embodiments, the NO of at least one filter medium x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 70% to 99% efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 75% to 99% efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 80% to 99% efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 85% to 99% efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 90% to 99% efficiency. x The removal efficiency is the initial NO x Efficiency is maintained in the range of 95% to 99%.

[0092] In some embodiments, the NO of at least one filter medium x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 70% to 95% of its efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 70% to 90% efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 70% to 85% of its efficiency. x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 70% to 80% of its efficiency. x The removal efficiency is the initial NO x It is maintained within the range of 70% to 75% of efficiency.

[0093] In some embodiments, the NO of at least one filter medium x The removal efficiency is the initial NO x In some embodiments, the NOx of at least one filter medium is maintained in the range of 75% to 95% of its efficiency. x The removal efficiency is the initial NO x Efficiency is maintained in the range of 80% to 90%.

[0094] In some embodiments, the concentration of SO2 in the flue gas stream is determined by the NO2 concentration in at least one filter medium. x Not exceeding 1000 ppm during the process to maintain removal efficiency (i.e., initial NO x As a percentage of efficiency, constant NO x In some embodiments, the concentration of SO2 in the flue gas stream is determined by the NO2 concentration in at least one filter medium. x The removal efficiency (i.e., initial NO x In some embodiments, the concentration of SO2 in the flue gas stream is maintained at 500 ppm during the step of maintaining the NOx efficiency of at least one filter medium (as a percentage of efficiency, as a constant NOx efficiency, or a combination thereof). x The removal efficiency (i.e., initial NO x As a percentage of efficiency, constant NO x In some embodiments, the concentration of SO2 in the flue gas stream is maintained at 250 ppm during the step of maintaining the concentration of SO2 in the flue gas stream at 250 ppm during the step of maintaining the concentration of NO2 in the at least one filter medium. x The removal efficiency (i.e., initial NO x As a percentage of efficiency, constant NO x In some embodiments, the concentration of SO2 in the flue gas stream is maintained at 100 ppm during the step of maintaining the concentration of SO2 in the flue gas stream at 100 ppm during the step of maintaining the concentration of NO2 in the at least one filter medium. x In some embodiments, the concentration of SO2 in the flue gas stream is adjusted to not exceed 75 ppm during the process to maintain the removal efficiency. x In some embodiments, the concentration of SO2 in the flue gas stream is greater than or equal to 50 ppm during the process to maintain the removal efficiency.x In some embodiments, the concentration of SO2 in the flue gas stream is greater than or equal to 25 ppm during the process to maintain the removal efficiency. x In some embodiments, the concentration of SO2 in the flue gas stream is adjusted to 12 ppm or less during the process to maintain the removal efficiency. x During the process to maintain the removal efficiency, the concentration of SO2 in the flue gas stream does not exceed 10 ppm. In some embodiments, the concentration of SO2 in the flue gas stream is reduced by at least one of the NO2 in the filter media. x In some embodiments, the concentration of SO2 in the flue gas stream is greater than or equal to 5 ppm during the process to maintain the removal efficiency. x In some embodiments, the concentration of SO2 in the flue gas stream is greater than or equal to 2 ppm during the process to maintain the removal efficiency of at least one filter medium. x The removal efficiency will not exceed 1 ppm during the process.

[0095] In some embodiments, the flue gas stream is at a first temperature during flow of the flue gas stream, and NO x Efficiency is maintained by increasing the temperature of the flue gas stream from a first temperature to a second temperature that is greater than the first temperature (i.e., the initial NO x As a percentage of efficiency or as a constant NO x efficiency or a combination thereof).

[0096] In some embodiments, the first temperature is in the range of 180°C to 230°C. In some embodiments, the first temperature is in the range of 190°C to 230°C. In some embodiments, the first temperature is in the range of 200°C to 230°C. In some embodiments, the first temperature is in the range of 210°C to 230°C. In some embodiments, the first temperature is in the range of 220°C to 230°C.

[0097] In some embodiments, the first temperature is in the range of 180°C to 220°C. In some embodiments, the first temperature is in the range of 180°C to 210°C. In some embodiments, the first temperature is in the range of 180°C to 200°C. In some embodiments, the first temperature is in the range of 180°C to 190°C.

[0098] In some embodiments, the first temperature is in the range of 190° C. to 220° C. In some embodiments, the first temperature is in the range of 200° C. to 210° C.

[0099] In some embodiments, the second temperature is at least 10° C. higher than the first temperature. In some embodiments, the second temperature is at least 20° C. higher than the first temperature. In some embodiments, the second temperature is at least 30° C. higher than the first temperature. In some embodiments, the second temperature is at least 40° C. higher than the first temperature. In some embodiments, the second temperature is at least 50° C. higher than the first temperature. In some embodiments, the second temperature is at least 60° C. higher than the first temperature. In some embodiments, the second temperature is at least 70° C. higher than the first temperature. In some embodiments, the second temperature is at least 80° C. higher than the first temperature. In some embodiments, the second temperature is at least 90° C. higher than the first temperature. In some embodiments, the second temperature is at least 100° C. higher than the first temperature.

[0100] In some embodiments, the second temperature is 10° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 20° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 30° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 40° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 50° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 60° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 70° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 80° C. to 100° C. higher than the first temperature. In some embodiments, the second temperature is 90° C. to 100° C. higher than the first temperature.

[0101] In some embodiments, the second temperature is 10° C. to 90° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 80° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 70° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 60° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 50° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 40° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 30° C. higher than the first temperature. In some embodiments, the second temperature is 10° C. to 20° C. higher than the first temperature.

[0102] In some embodiments, the second temperature is 20° C. to 90° C. higher than the first temperature. In some embodiments, the second temperature is 30° C. to 80° C. higher than the first temperature. In some embodiments, the second temperature is 40° C. to 70° C. higher than the first temperature. In some embodiments, the second temperature is 50° C. to 60° C. higher than the first temperature.

[0103] In some embodiments, the second temperature is at least 240°C. In some embodiments, the second temperature is at least 245°C. In some embodiments, the second temperature is at least 250°C. In some embodiments, the second temperature is at least 255°C. In some embodiments, the second temperature is at least 260°C. In some embodiments, the second temperature is at least 265°C. In some embodiments, the second temperature is at least 270°C. In some embodiments, the second temperature is at least 275°C. In some embodiments, the second temperature is at least 280°C.

[0104] In some embodiments, the second temperature is at most 280°C. In some embodiments, the second temperature is at most 275°C. In some embodiments, the second temperature is at most 270°C. In some embodiments, the second temperature is at most 265°C. In some embodiments, the second temperature is at most 260°C. In some embodiments, the second temperature is at most 255°C. In some embodiments, the second temperature is at most 250°C. In some embodiments, the second temperature is at most 245°C. In some embodiments, the second temperature is at most 240°C.

[0105] In some embodiments, the second temperature is in the range of 240°C to 280°C. In some embodiments, the second temperature is in the range of 240°C to 275°C. In some embodiments, the second temperature is in the range of 240°C to 270°C. In some embodiments, the second temperature is in the range of 240°C to 265°C. In some embodiments, the second temperature is in the range of 240°C to 260°C. In some embodiments, the second temperature is in the range of 240°C to 255°C. In some embodiments, the second temperature is in the range of 240°C to 250°C. In some embodiments, the second temperature is in the range of 240°C to 245°C.

[0106] In some embodiments, the second temperature is in the range of 240°C to 275°C. In some embodiments, the second temperature is in the range of 240°C to 270°C. In some embodiments, the second temperature is in the range of 240°C to 265°C. In some embodiments, the second temperature is in the range of 240°C to 260°C. In some embodiments, the second temperature is in the range of 240°C to 255°C. In some embodiments, the second temperature is in the range of 240°C to 250°C. In some embodiments, the second temperature is in the range of 240°C to 245°C.

[0107] In some embodiments, the second temperature is in the range of 245° C. to 275° C. In some embodiments, the second temperature is in the range of 250° C. to 270° C. In some embodiments, the second temperature is in the range of 255° C. to 265° C.

[0108] In some embodiments, NH is converted to NO in the flue gas stream while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x The NH3 is added in a concentration ratio of 1:100 to 5:1 based on the concentration of the compound. In some embodiments, while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature, the NH3 is added to the NO3 in the flue gas. x The NH3 is added in a concentration ratio of 1:50 to 5:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and the NH3 is added in a concentration ratio of 1:25 to 5:1 based on the concentration of the compounds. In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 ... x The NH3 is added in a concentration ratio of 1:10 to 5:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. xThe NH3 is added in a concentration ratio of 1:5 to 5:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x The NH3 is added in a concentration ratio of 1:2 to 5:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x Compounds are added at concentration ratios ranging from 1:1 to 5:1 based on their concentration.

[0109] In some embodiments, NH is converted to NO in the flue gas stream while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x The NH3 is added in a concentration ratio of 1:100 to 2:1 based on the concentration of the compounds. In some embodiments, the NH3 is added to the NO3 in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x The NH3 is added in a concentration ratio of 1:100 to 1:5 based on the concentration of the compound. In some embodiments, while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature, the NH3 is added to the NO3 in the flue gas. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x The compounds are added at a concentration ratio of 1:100 to 1:50 based on their concentration. In some embodiments, NH is converted to NO in the flue gas while the temperature of the flue gas stream is increased from a first temperature to a second temperature that is greater than the first temperature. x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH7 into NH8 into NH9 into NH10 into NH3, and the NH3 is added in a concentration ratio of 1:50 to 2:1 based on the concentration of the compounds. In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH5 into NH6 into NH3, and the NH3 is added in a concentration x In some embodiments, NH3 is added to the flue gas to convert NO3 into NH4 into NH3. x Compounds are added at a concentration ratio of 1:10 to 1:2 based on their concentration.

[0110] In some embodiments, even if NH3 is not present in the flue gas stream, NO x Removal efficiency is maintained. In some embodiments, the first temperature is increased to the second temperature without adding NH3 to the flue gas stream.

[0111] In some embodiments, the first temperature is raised to the second temperature for 0.25 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 0.5 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 1 hour to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 2 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 5 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 10 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 12 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 24 hours to 48 hours. In some embodiments, the first temperature is raised to the second temperature for 36 hours to 48 hours.

[0112] In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 36 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 24 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 12 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 10 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 5 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 2 hours. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 1 hour. In some embodiments, the first temperature is increased to the second temperature for 0.25 hours to 0.5 hours.

[0113] In some embodiments, the first temperature is raised to the second temperature for between 0.5 hours and 36 hours. In some embodiments, the first temperature is raised to the second temperature for between 1 hour and 24 hours. In some embodiments, the first temperature is raised to the second temperature for between 2 hours and 12 hours. In some embodiments, the first temperature is raised to the second temperature for between 5 hours and 10 hours.

[0114] In some embodiments, the first temperature is increased to the second temperature intermittently, hi some embodiments, the first temperature is increased to the second temperature continuously.

[0115] In some embodiments, the intermittent increases occur at fixed time intervals. In some embodiments, the intermittent increases occur at variable time intervals. In some embodiments, the intermittent increases occur at random time intervals.

[0116] In some embodiments, the intermittent ramping includes ramping the first temperature to the second temperature for a predetermined period of time (e.g., as described above) and ramping the second temperature back down to the first temperature after the predetermined period of time, hi some embodiments, the intermittent ramping includes periodically performing the aforementioned steps.

[0117] In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 10 to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 100 to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1,000 to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 5,000 to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 10,000 to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 20,000 to 40,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 30,000 to 40,000 hours.

[0118] In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 30,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 20,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 10,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 5,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 1,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 100 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1 hour to 10 hours.

[0119] In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 10-30,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 100-20,000 hours. In some embodiments, the intermittent increase includes increasing the first temperature to the second temperature every 1,000-5,000 hours.

[0120] 1A-1D show exemplary filter media embodiments according to the present disclosure.

[0121] 1A, at least one filter media 101 may be contained within at least one filter bag 100. A flue gas stream 102 may flow through the at least one filter media 101 by passing through cross section A. As the gas stream 102 flows through the at least one filter media 101, the flue gas stream 102 may flow adjacent to the at least one filter bag, as indicated by the vertical arrows.

[0122] FIG. 1B illustrates an exemplary filter medium 101 according to some embodiments of the present disclosure. As shown in FIG.x A flue gas flow 102, which may include chemical compounds and solid particles 107, may flow through cross section A from an upstream side 103 of the filter media 101 to a downstream side 104 of the filter media. Although not shown, the upstream side 103 of the filter media 101 may correspond to the outside of a filter bag, such as the filter bag 100, in some embodiments. Similarly, the downstream side 104 of the filter media 101 may correspond to the inside of a filter bag, such as the filter bag 100. In some embodiments, the filter media 101 includes at least one protective membrane 106 and one or more felt batts 108 on one of the upstream side 103 of the filter media 101, the downstream side 104 of the filter media 101, or any combination thereof. In some embodiments, the one or more felt batts 108 may be disposed on the porous catalyst film 105. In some embodiments, the combination of the one or more felt batts 108 and the porous catalyst film 105 may be referred to as a porous catalyst layer (not shown in FIG. 1B).

[0123] 1C illustrates a non-limiting exemplary embodiment of a porous catalyst film 105. As shown, the porous catalyst film 105 can include catalyst particles 109 on at least one surface of the porous catalyst film 105. An ABS deposit 110 can be disposed on the surface of the catalyst particles 109.

[0124] FIG. 1D illustrates a further non-limiting exemplary embodiment of the filter media 101. As shown, the filter media 101 can include a porous catalyst layer 111. In some non-limiting embodiments, the filter media 101 can take the form of a filter bag. In some embodiments, the porous catalyst layer 111 can be coated with a catalytic material (not shown in FIG. 1D), such as catalytic particles. In some embodiments, the catalytic material can be attached to the porous catalyst layer 111 by one or more adhesives (not shown) as described herein. In some embodiments, the filter media 101 can include a porous protective membrane 106. EXAMPLES

[0125] Example 1: In-situ "flow-through" thermal regeneration of filter media containing catalytic filter bags with NO, NO2 and NH3 gas mixtures containing low levels of SO2

[0126] Four catalyzed filter bags (65 mm diameter, 1630 mm length) were prepared from the catalytic composite article described below.

[0127] A catalytic composite article was formed according to WO 2019 / 099025 to Eves et al. The filter media included a catalytic composite article having a polytetrafluoroethylene (PTFE) + catalyst composite membrane having a first upstream side and a second downstream side, and a catalyst layered assembly including one or more felt batts. Each felt batt was formed from a fleece formed from PTFE staple fibers. The filter media were connected by a plurality of perforations formed by a needle punching process, a needling process, or both.

[0128] The polytetrafluoroethylene (PTFE) + catalyst composite membrane of the above-mentioned filter media was prepared by forming a composite tape using the general dry blending method taught in Zhong et al., U.S. Patent No. 7,791,861 B2, and then uniaxially expanding according to the teachings of Gore, U.S. Patent No. 3,953,556. The resulting porous fibrillated expanded PTFE (ePTFE) composite membrane contained supported catalyst particles durably entangled and immobilized with the ePTFE node and fibril matrix.

[0129] NO before ammonium bisulfate (ABS) deposition x Reaction efficiency: The filter media, including the sample catalytic filter bag, was combusted with NOx from simulated flue gas at 230°C using Innovative Combustion Technologies. x The removal efficiency was tested. The simulated flue gas contained 200 ppm NO, 1.5 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23.3 standard cubic feet per minute (SCFM).x To determine the removal efficiency, the upstream concentrations of NO and NO2 (i.e., the NO entering the chamber before being exposed to the filter media) were x concentration) and downstream concentration (i.e., NO leaving the chamber after exposure to the filter media). x The NO concentration was monitored with an MKS MULTI-GAS™ 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). x The removal efficiency was calculated according to the following formula: x " indicates the total concentration of NO and NO2 in the respective streams.

[0130] In-situ deposition of ammonium bisulfate (ABS): The sample media containing the catalyzed filter bags were contaminated in situ with Innovative Combustion Technologies with 400 ppm NO, 440 ppm NH3, 3000 ppm SO2, and 8% moisture at a total flow rate of 23.3 standard cubic feet per minute (SCFM) for 4 hours at 230°C.

[0131] NO after ammonium bisulfate (ABS) deposition x Reaction efficiency: NO in catalyzed filter bags after ABS deposition x The removal efficiency was tested with "Innovative Combustion Technologies" from simulated flue gas at 230°C, as described above. The simulated flue gas contained 200 ppm NO, 1.5 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23.3 standard cubic feet per minute (SCFM).

[0132] On-site "flow-through" thermal regeneration with NO, NO2, NH3 and SO2 mixtures: During on-site thermal regeneration, a filter medium containing four catalytic filter bags contaminated on-site as described above was used, containing 7 ppm SO2, 200 ppm NO, 1 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2, NH3 / NO ratio of 1.0. x The ratio set gas mixture was first ramped to 260° C. and set to pass through the catalyzed filter bag for 8 hours at 260° C. with a total flow rate of 22.0 SCFM.

[0133] NO after thermal regeneration x Reaction efficiency: NO in catalytic filter bags after thermal regeneration x The removal efficiency was tested with "Innovative Combustion Technologies" from simulated flue gas at 230°C, as described above. The simulated flue gas contained 200 ppm NO, 1.5 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23.3 standard cubic feet per minute (SCFM).

[0134] result: Figure 2 shows the results of the thermal regeneration (NH3 / NO at 260 °C) of the catalyzed filter bag (1) before ammonium bisulfate (ABS) deposition, (2) after ABS deposition, and (3) x = 1.0, NO after 7 ppm SO2 mixture x Figure 2 shows the NO removal efficiency before ABS deposition. x The removal efficiency of NO after ABS deposition x Figure 2 shows that the NO removal efficiency after thermal regeneration is higher than that of the conventional NO removal method. x The removal efficiency of NO after ABS deposition x Figure 2 also shows that the NO removal efficiency before ABS deposition was higher than that before ABS deposition. x Removal efficiency is NO after thermal regeneration x This indicates that the removal efficiency is higher than that of the control.

[0135] Example 2 (comparative example): In-situ "flow-through" thermal regeneration of filter media containing catalytic filter bags with NO, NO2, NH3 and SO2 gas mixtures with higher SO2 concentrations

[0136] For this comparative example, four catalyzed filter bags (65 mm diameter, 1630 mm length) were prepared from the catalytic composite article as described above in Example 1.

[0137] NO before ammonium bisulfate (ABS) deposition x Reaction efficiency: The media containing the sample catalyzed filter bags were tested in an Innovative Combustion Technologies system from simulated flue gas at 230°C. The simulated flue gas contained 200 ppm NO, 1.5 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23.3 standard cubic feet per minute (SCFM). x To determine the removal efficiency, the upstream concentrations of NO and NO2 (i.e., the NO entering the chamber before being exposed to the filter media) were x concentration) and downstream concentration (i.e., NO leaving the chamber after exposure to the filter media). x The NO concentration was monitored with an MKS MULTI-GAS™ 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). x The removal efficiency was calculated according to the following formula: x " indicates the total concentration of NO and NO2 in the respective streams.

[0138] In-situ deposition of ammonium bisulfate (ABS): The filter media containing the sample catalyzed filter bags were contaminated in situ at Innovative Combustion Technologies with 400 ppm NO, 440 ppm NH3, 3000 ppm SO2 and 8% moisture at a total flow rate of 23.3 standard cubic feet per minute (SCFM) for 4 hours at 230°C.

[0139] NO after ammonium bisulfate (ABS) deposition x Reaction efficiency: NO in catalyzed filter bags after ABS deposition x The removal efficiency was tested with "Innovative Combustion Technologies" from simulated flue gas at 230°C, as described above. The simulated flue gas contained 200 ppm NO, 1.5 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23.3 standard cubic feet per minute (SCFM).

[0140] On-site "flow-through" thermal regeneration with NO, NO2, NH3 and SO2 gas mixtures: During on-site thermal regeneration, a filter medium containing four catalytic filter bags contaminated on-site as described above was used, containing 200 ppm NO, 1 ppm NO2, 200 ppm NH3, 12 ppm SO2, 10% O2, 8% moisture and N2, with a NH3 / NO ratio of 1.0. x The ratio set gas mixture was first ramped to 260° C. and set to pass through the catalyzed filter bag for 18 hours at 260° C. with a total flow rate of 22.0 SCFM.

[0141] NO after thermal regeneration x Reaction efficiency: NO in catalytic filter bags after thermal regeneration x The removal efficiency was tested with "Innovative Combustion Technologies" from simulated flue gas at 230°C, as described above. The simulated flue gas contained 200 ppm NO, 1.5 ppm NO2, 200 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23.3 standard cubic feet per minute (SCFM).

[0142] Comparative example results: Figure 3 shows the results of the catalyzed filter bag (1) before ammonium bisulfate (ABS) deposition, (2) after ABS deposition, and (3) thermal regeneration (NH3 / NO x = 1.0, NO after 12 ppm SO2 mixture x Figure 3 shows the NO removal efficiency before ABS deposition. xRemoval efficiency is NO after ABS deposition x Figure 3 shows that the NO removal efficiency after thermal regeneration is higher than that of the conventional method. x Removal efficiency of NO after ABS deposition x Figure 3 also shows that the NO removal efficiency before ABS deposition is not higher than that of the x Removal efficiency is NO after thermal regeneration x This indicates that the removal efficiency is higher than that of the control.

[0143] Example 3: In-situ "flow-through" thermal regeneration of media containing catalytic filter bags with NO, NO2 and NH3 gas mixture at 260°C

[0144] Four catalytic filter bags (65 mm diameter, 1630 mm length) were prepared from the catalytic composite article as described in Example 1.

[0145] NO before ammonium bisulfate (ABS) deposition x Reaction efficiency: The sample catalyst filter bag containing the filter media was used to extract NO from simulated flue gas at 230°C using Innovative Combustion Technologies. x The removal efficiency was tested. The simulated flue gas contained 400 ppm NO, 4 ppm NO2, 400 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23 standard cubic feet per minute (SCFM). x To determine the removal efficiency, the upstream concentrations of NO and NO2 (i.e., the NO entering the chamber before being exposed to the filter media) were x concentration) and downstream concentration (i.e., NO leaving the chamber after exposure to the filter media). x The NO concentration was monitored with an MKS MULTI-GAS™ 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). x The removal efficiency was calculated according to the following formula: x " indicates the total concentration of NO and NO2 in the respective streams.

[0146] In-situ deposition of ammonium bisulfate (ABS): The media containing the sample catalyzed filter bags were contaminated in situ with 400 ppm NO, 450 ppm NH, 3000 ppm SO and 8% moisture at 230°C for 4 hours in an Innovative Combustion Technologies facility with a total flow rate of 23 standard cubic feet per minute (SCFM).

[0147] NO after ammonium bisulfate (ABS) deposition x Reaction efficiency: NO in catalyzed filter bags after ABS deposition x The removal efficiency was tested with "Innovative Combustion Technologies" from simulated flue gas at 230°C, as described above. The simulated flue gas contained 400 ppm NO, 5 ppm NO2, 450 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 23 standard cubic feet per minute (SCFM).

[0148] In-situ "flow-through" thermal regeneration with NO, NO2 and NH3 mixtures: During on-site thermal regeneration, a filter medium containing four catalytic filter bags contaminated on-site as described above was used, containing <1 ppm SO2, 400 ppm NO, 5 ppm NO2, 450 ppm NH3, 10% O2, 8% moisture and 1.1 NH3 / NO2. x The ratio set gas mixture was first ramped to 260°C and set to pass through the catalyzed filter bag at 260°C for 2 hours with a total flow rate of 24 SCFM.

[0149] NO after thermal regeneration x Reaction efficiency: NO in catalyzed filter bags after 2 hours of thermal regeneration with NH3 xThe removal efficiency was tested with "Innovative Combustion Technologies" from simulated flue gas at 260°C, as described above. The simulated flue gas contained 400 ppm NO, 4 ppm NO2, 400 ppm NH3, 10% O2, 8% moisture and N2 with a total flow rate of 24 standard cubic feet per minute (SCFM).

[0150] NO in catalytic filter bags after thermal regeneration x The removal efficiency was later tested with "Innovative Combustion Technologies" from simulated flue gas at 230°C, as described above. The simulated flue gas contained 400 ppm NO, 2 ppm NO2, 400 ppm NH3, 10% O2, 8% moisture and N2, with a total flow rate of 23 standard cubic feet per minute (SCFM).

[0151] result: Figure 4 shows the results of the thermal regeneration (NH3 / NO at 260 °C) of the catalyzed filter bag (1) before ammonium bisulfate (ABS) loading, (2) after ABS loading, and (3) x = 1.1, with <1 ppm SO2 mixture) x Figure 4 shows the NO removal efficiency before ABS deposition. x The NOx removal efficiency after thermal regeneration is higher than that after ABS deposition. x Removal efficiency is NO after ABS deposition x Figure 4 also shows that the NO removal efficiency before ABS deposition is higher than that before ABS deposition. x Removal efficiency is NO after thermal regeneration x Higher removal efficiency, but thermal regeneration NO x The removal efficiency value is NO before ABS deposition x It can be seen that the values ​​are almost close to the removal efficiency values.

[0152] Example 4: In-situ "flow-through" thermal regeneration of media containing catalytic filter bags with NO, NO2 and NH3 gas mixture at 245°C

[0153] Four catalyzed filter bags (65 mm diameter, 1630 mm length) were prepared from the catalytic composite article as described in Example 1.

[0154] In-situ deposition of ammonium bisulfate (ABS) The sample media containing the catalyzed filter bags were contaminated by Innovative Combustion Technologies with 400 ppm NO, 440 ppm NH3, 3000 ppm SO2 and 8% moisture at 230°C for 4 hours with a total flow rate of 23.3 standard cubic feet per minute (SCFM).

[0155] NO prior to in-situ "flow-through" thermal regeneration with a mixture of NO, NO2 and NH3 x Reaction efficiency: The returned catalytic filter bag extracts catalytic NO from the simulated flue gas. x The samples were tested for removal efficiency. Briefly, a 30 mm diameter sample was placed in a sample holder located in a 3210 series furnace (Applied Test Systems). The samples were exposed to simulated flue gas with N2 balance at 232 °C. The simulated flue gas contained 244 ppm NO, 1 ppm NO2, 200 ppm NH3, 6% O2 and N2 with a total flow rate of 0.62 L / min. NO x To determine the removal efficiency, x The upstream and downstream concentrations (i.e., relative to the catalytic composite article) of NO were monitored with an MKS MULTI-GAS™ 2030D FTIR analyzer (MKS Instruments, Andover, Mass.). x The removal efficiency was calculated according to the following formula: x " indicates the total concentration of NO and NO2 in the respective streams.

[0156] In-situ "flow-through" thermal regeneration with NO, NO2 and NH3 mixtures: During the in-situ thermal regeneration, 30 mm diameter samples were placed in a sample holder located in a 3210 series furnace (Applied Test Systems). The samples were exposed to N2-balanced simulated flue gas at 245 °C for 33 h. The simulated flue gas contained 244 ppm NO, 1 ppm NO2, 60 ppm NH3, 6% O2, 5% moisture and N2 with a total flow rate of 0.62 L / min.

[0157] NO after thermal regeneration x Reaction efficiency: NO after 33 hours of thermal regeneration with NH x The removal efficiency was again tested from simulated flue gas at 232° C. as above. The simulated flue gas contained 244 ppm NO, 1 ppm NO2, 200 ppm NH3, 6% O2 and N2, with a total flow rate of 0.62 L / min.

[0158] result: Figure 5 shows the NO (1) after ABS deposition and (2) after thermal regeneration (245 °C in the presence of NH3). x The Y-axis in Figure 5 shows the NO removal efficiency in the range of 68.5% to 72.0%. x The removal efficiency of NO before ABS deposition is shown in Fig. 5. x The removal efficiency is the NO removal efficiency after ABS deposition. x It will be understood that the NO removal efficiency is higher than that of the NO removal efficiency after thermal regeneration. x Removal efficiency of NO after ABS deposition x This indicates that the removal efficiency is higher than that of the control.

[0159] Aspects:

[0160] Various aspects are described below. Any of the following aspects, or any portion thereof, can be combined with any of the other aspects, or any portion thereof. Aspect 1.: Providing at least one filter medium; wherein the at least one filter medium is at least one catalytic material; and Ammonium bisulfate (ABS), ammonium sulfate (AS) or any combination thereof; Including, flowing the flue gas stream through or adjacent to at least one filter medium; wherein the flue gas stream comprises: Nitric oxide (NO), and Nitrogen dioxide (NO2) Contains NO x a compound, the flue gas stream being at a first temperature during the flow process; NO of the at least one filter medium x Increasing the removal efficiency; wherein the NO of the at least one filter medium x Increasing the removal efficiency means adding ammonia (NH3) at a concentration in the range of 0.0001% to 0.5% of the concentration of the flue gas stream; and increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature. The method comprises the steps of: regenerating said at least one filter medium. Aspect 2. The method of aspect 1, wherein the second temperature is at least 10° C. higher than the first temperature. Aspect 3: The method according to aspect 1 or 2, wherein the second temperature is 10°C to 100°C higher than the first temperature. Embodiment 4: The method of any one of the preceding embodiments or any combination thereof, wherein the first temperature is in the range of 180°C to 230°C. Embodiment 5: The method of any one of the preceding embodiments or combinations thereof, wherein the second temperature is at least 240°C. Embodiment 6: The method of any one of the preceding embodiments or any combination thereof, wherein the second temperature is up to 280°C. Embodiment 7: The method of any one of the preceding embodiments or any combination thereof, wherein the second temperature is in the range of 240°C to 280°C. Embodiment 8: The method of any one of the preceding embodiments or any combination thereof, wherein the second temperature is in the range of 240°C to 260°C. Embodiment 9. The method of any one of the preceding embodiments or any combination thereof, wherein the flue gas stream further comprises at least one of oxygen (O2), water (H2O), nitrogen (N2), carbon monoxide (CO), sulfur dioxide (SO2), sulfur trioxide (SO3), one or more hydrocarbons, or any combination thereof. Embodiment 10: The method of any one of the preceding embodiments or any combination thereof, wherein the flue gas flow is caused to flow across a cross-section of at least one filter medium such that the flue gas flow passes through the cross-section of at least one filter medium. Aspect 11: The method of any one of aspects 1 to 10 or any combination thereof, wherein the flue gas flow is not passed across a cross-section of the at least one filter medium such that the flue gas flow does not pass through a cross-section of the at least one filter medium. Aspect 12: The method of aspect 10, wherein the flue gas stream is flowed perpendicular to a cross-section of the at least one filter medium. Aspect 13: The method of aspect 11, wherein the flue gas stream is flowed parallel to a cross-section of the at least one filter medium. Aspect 14: The method of any one of aspects 1 to 10, 12, or any combination thereof, wherein the at least one filter medium is disposed within at least one filter bag, the at least one filter bag is contained within at least one filter bag housing, and the at least one catalytic material is in the form of catalytic particles. Aspect 15: The method of any one of claims 1 to 11, 13, or a combination thereof, wherein the at least one filter medium comprises a porous protective layer and a porous catalyst layer, the porous catalyst layer comprising at least one catalytic material. Aspect 16: The method of aspect 15, wherein the porous protective layer comprises a microporous layer, the microporous layer comprising an expanded polytetrafluoroethylene (ePTFE) membrane. Embodiment 17: The method of any one of the preceding embodiments or any combination thereof, wherein the at least one catalytic material is adhered to the filter media by at least one adhesive. Aspect 18: The method of Aspect 17, wherein the at least one adhesive is selected from polytetrafluoroethylene (PTFE), fluorinated ethylene propylene (FEP), high molecular weight polyethylene (HMWPE), high molecular weight polypropylene (HMWPP), perfluoroalkoxyalkane (PFA), polyvinylidene fluoride (PVDF), vinylidene fluoride (THV), chlorofluoroethylene (CFE), or any combination thereof. Example 19. The method of any one of Examples 15 to 18, or any combination thereof, wherein the porous catalyst layer comprises at least one polymer substrate. Aspect 20: The method of Aspect 19, wherein the at least one polymer substrate comprises at least one of polytetrafluoroethylene, poly(ethylene-co-tetrafluoroethylene), ultra-high molecular weight polyethylene, polyparaxylylene, polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, glass fiber, or any combination thereof. Aspect 21: The method of aspect 15, wherein the porous catalyst layer is in the form of a layered assembly comprising a porous catalyst film and one or more felt batts, the one or more felt batts being disposed on at least one side of the porous catalyst film. Aspect 22: The method of aspect 21, wherein the one or more felt batts comprise at least one of polytetrafluoroethylene (PTFE) felt, PTFE fleece, expanded polytetrafluoroethylene (ePTFE) felt, ePTFE fleece, woven fluoropolymer staple fibers, nonwoven fluoropolymer staple fibers, or any combination thereof. Example 23: The method of any one of Examples 21, 22, or any combination thereof, wherein the porous catalyst film comprises an expanded polytetrafluoroethylene (ePTFE) membrane. Example 24. The method of any one of Examples 14, 22-23, or any combination thereof, wherein the catalyst particles are entangled within the porous catalyst layer. Aspect 25: The method of any one of aspects 15 to 24, or any combination thereof, wherein the porous catalyst layer comprises at least one of polytetrafluoroethylene (PTFE), poly(ethylene-co-tetrafluoroethylene) (ETFE), ultra-high molecular weight polyethylene (UHMWPE), polyparaxylylene (PPX), polylactic acid, polyimide, polyamide, polyaramid, polyphenylene sulfide, and glass fiber, or any combination thereof. Embodiment 26. The method of any one of the preceding embodiments or any combination thereof, wherein the at least one catalytic material comprises one of vanadium monoxide (VO), vanadium trioxide (VO), vanadium dioxide (VO), vanadium pentoxide (VO), tungsten trioxide (WO), molybdenum trioxide (MoO), titanium dioxide (TiO), silicon dioxide (SiO), aluminum trioxide (AlO), manganese oxide (MnO), a zeolite, or any combination thereof. Embodiment 27: The method of any one of the preceding embodiments or any combination thereof, wherein the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 99% by weight of the at least one filter medium during the providing step. Embodiment 28: The method of any one of the preceding embodiments or any combination thereof, wherein the ABS deposit is disposed on the catalytic material of the at least one filter medium at a concentration ranging from 0.01% to 98% by weight of the at least one filter medium after the raising step. Aspect 29: NO of the at least one filter medium x The method of any one of the preceding embodiments, or any combination thereof, wherein the removal efficiency is at least 0.5% higher after the raising step than during the providing step. Aspect 30: The method of any one of the preceding aspects or any combination thereof, 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. Aspect 31: NO x The method of any one of the preceding embodiments, or any combination thereof, wherein increasing the removal efficiency comprises removing at least a portion of the ABS deposits, the AS deposits, or any combination thereof from the at least one filter medium. Aspect 32: providing at least one filter medium; wherein the at least one filter medium comprises at least one catalytic material. flowing the flue gas flow across a cross-section of the at least one filter medium such that the flue gas flow 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: Nitric oxide (NO), and Nitrogen dioxide (NO2), Contains NO x compound, Sulfur dioxide (SO2), and Ammonia (NH3), wherein the flue gas stream is at a first temperature during the flow process; and A certain NO of the at least one filter medium x Maintaining removal efficiency; wherein the at least one filter medium has a constant NO x maintaining the removal efficiency includes increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature. 1. A method for scrubbing a flue gas stream, comprising: Aspect 33: At least during the flow process, SO2, NH3 and NO x The compound is at least 1 mg / m based on the total volume of the flue gas stream. 3 The method of embodiment 32, wherein the compound is present in an amount of Embodiment 34: The method of any one of embodiments 32, 33, or any combination thereof, wherein the second temperature is at least 10° C. higher than the first temperature. Embodiment 35: The method of any one of embodiments 32 to 34 or any combination thereof, wherein the second temperature is 10°C to 100°C higher than the first temperature. Embodiment 36: A method according to any one of embodiments 32 to 35 or any combination thereof, wherein the first temperature is in the range of 180°C to 230°C. Embodiment 37: The method of any one of embodiments 32 to 36, or any combination thereof, wherein the second temperature is at least 240°C. Embodiment 38: The method of any one of embodiments 32 to 37 or any combination thereof, wherein the second temperature is up to 280°C. Embodiment 39: A method according to any one of embodiments 32 to 38 or any combination thereof, wherein the second temperature is in the range of 240°C to 280°C. Embodiment 40: The method of any one of embodiments 32 to 39 or any combination thereof, wherein the second temperature is in the range of 240°C to 260°C. Aspect 41. The method of any one of Aspects 32 to 40, or any combination thereof, wherein during the maintaining step, the concentration of SO2 in the flue gas stream does not exceed 1000 ppm. Aspect 42: The method of any one of aspects 32 to 41, or any combination thereof, wherein during the maintaining step, the concentration of SO2 in the flue gas stream does not exceed 10 ppm. Aspect 43: providing at least one filter medium; wherein the at least one filter medium comprises at least one catalytic material. flowing the flue gas stream adjacent a cross-section of the at least one filter medium such that the flue gas stream flows parallel to 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: Nitric oxide (NO), and Nitrogen dioxide (NO2), Contains NO x compound, Sulfur dioxide (SO2), and Ammonia (NH3), Including, wherein the flue gas stream is at a first temperature during a flow process. A constant NO of at least one filter medium x Maintaining removal efficiency; A certain NO of the at least one filter medium x maintaining the removal efficiency includes increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature. 1. A method for scrubbing a flue gas stream, comprising: Aspect 44.: At least during the flow process, SO2, NH3 and NO x The compound is at least 1 mg / m based on the total volume of the flue gas stream. 3 The method of embodiment 43, wherein the compound is present in an amount of Aspect 45.: The method of any one of Aspects 43 or 44, 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. Embodiment 46: The method of any one of embodiments 43 to 45 or any combination thereof, wherein the second temperature is at least 10° C. higher than the first temperature. Embodiment 47: The method of any one of embodiments 43 to 46 or any combination thereof, wherein the second temperature is 10°C to 100°C higher than the first temperature. Embodiment 48: The method of any one of embodiments 43 to 47 or any combination thereof, wherein the first temperature is in the range of 180°C to 230°C. Embodiment 49: Any one of embodiments 43 to 48 or any method thereof, wherein the second temperature is at least 240°C. Embodiment 50: The method of any one of embodiments 43 to 49 or any combination thereof, wherein the second temperature is up to 280°C. Embodiment 51: The method described in any one of embodiments 43 to 50 or any of the above, wherein the second temperature is in the range of 240°C to 280°C. Embodiment 52: A method according to any one of embodiments 43 to 51 or any combination thereof, wherein the second temperature is in the range of 240°C to 260°C. Embodiment 53: The method of any one of embodiments 43 to 52, or any combination thereof, wherein during the maintaining step, the concentration of SO2 in the flue gas stream does not exceed 1000 ppm. Embodiment 54. The method of any one of embodiments 43 to 52, or any combination thereof, wherein during the maintaining step, the concentration of SO2 in the flue gas stream does not exceed 10 ppm. Aspect 55: NO x Initial NO removal efficiency x 55. The method of any one of the preceding claims or any combination thereof, wherein the first temperature of the flue gas stream is intermittently increased to the second temperature so as to maintain an efficiency of at least 70%. Embodiment 56: The method of embodiment 55, wherein intermittently increasing includes increasing the first temperature to the second temperature every 1 hour to 40,000 hours. Embodiment 57. The method of any one of embodiments 55, 56, or any combination thereof, wherein the intermittent increasing occurs at regular time intervals. Embodiment 58. The method of any one of embodiments 55, 56, or any combination thereof, wherein the intermittent increasing occurs at variable time intervals. Aspect 59.: The method of aspect 58, wherein the variable time interval is a random time interval. Aspect 60.:NO x Initial NO removal efficiency x 60. The method of any one of the preceding claims or any combination thereof, wherein the first temperature of the flue gas stream is continuously increased to the second temperature to maintain an efficiency of at least 70%. Aspect 61.: providing at least one filter medium; wherein the at least one filter medium comprises at least one catalytic material. flowing the flue gas flow across a cross-section of the at least one filter medium such that the flue gas flow 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: Nitric oxide (NO), and Nitrogen dioxide (NO2), Contains NO x compound, Sulfur dioxide (SO2), and Ammonia (NH3), Including, wherein the flue gas stream is at a first temperature during a flow process. The at least one filter medium is provided with a filter member having a first temperature and a second temperature, the second temperature being greater than the first temperature. x Initial NO removal efficiency x maintain at least 70% of its efficiency; 1. A method for scrubbing a flue gas stream, comprising: Aspect 62: NO of the at least one filter medium x Removal efficiency is the initial NO x The method of embodiment 61, wherein the efficiency is maintained in the range of 70% to 99%. Embodiment 63: The method of any one of embodiments 61 or 62, wherein the second temperature is at least 10° C. higher than the first temperature. Embodiment 64: A method according to any one of embodiments 61 to 63 or any combination thereof, wherein the second temperature is 10°C to 100°C higher than the first temperature. Embodiment 65: A method according to any one of embodiments 61 to 64 or any combination thereof, wherein the first temperature is in the range of 180°C to 230°C. Embodiment 66: The method of any one of embodiments 61 to 65 or any combination thereof, wherein the second temperature is at least 240°C. Embodiment 67: The method of any one of embodiments 61 to 66 or any combination thereof, wherein the second temperature is up to 280°C. Embodiment 68: A method according to any one of embodiments 61 to 67 or any combination thereof, wherein the second temperature is in the range of 240°C to 280°C. Embodiment 69: A method according to any one of embodiments 61 to 68 or any combination thereof, wherein the second temperature is in the range of 240°C to 260°C. Aspect 70. The method of any one of aspects 61 to 69 or any combination thereof, wherein during the maintaining step, the concentration of SO2 in the flue gas stream does not exceed 1000 ppm. Embodiment 71: The method of any one of embodiments 61 to 70, or any combination thereof, wherein during the maintaining step, the concentration of SO2 in the flue gas stream does not exceed 10 ppm. Aspect 72.: The concentration of SO2 in the flue gas stream is determined by the NO2 concentration in the at least one filter medium. x 32. The method of any one of embodiments 1 to 31 or any combination thereof, wherein the removal efficiency during the step of increasing the removal efficiency does not exceed 1000 ppm. Aspect 73.: The concentration of SO2 in the flue gas stream is determined by the NO2 concentration in the at least one filter medium. x 73. The method of any one of embodiments 1 to 31, or any combination thereof, wherein the removal efficiency during the step of increasing the removal efficiency does not exceed 10 ppm.

[0161] Variations, modifications, and alterations to the embodiments of the present disclosure described above will be apparent to those of ordinary skill in the art. All such variations, modifications, alterations, and the like are intended to fall within the spirit and scope of the disclosure, which is limited only by the appended claims.

[0162] Although several embodiments of the present disclosure have been described, it is understood that these embodiments are exemplary only and not limiting, and that many variations may become apparent to one skilled in the art. For example, all dimensions discussed herein are provided by way of example only and are for illustrative purposes and are not intended to be limiting.

[0163] Any features or elements explicitly identified in this description may be explicitly excluded as features or elements of an embodiment of the invention as defined in the claims.

[0164] The disclosure described herein can be implemented without one or more elements or one or more limitations not specifically disclosed herein. Thus, for example, in each example of this specification, any of the terms "comprise", "essentially consist of" and "consist of" can be replaced with either of the other two terms. The terms and expressions used are used as terms of description, not of limitation, and in the use of such terms and expressions, there is no intention to exclude the features shown and described or equivalent forms of some of them, and it should be noted that various modifications are possible within the scope of this disclosure.

Claims

1. providing at least one filter medium; wherein the at least one filter medium is At least one catalytic material; and Ammonium bisulfate (ABS), ammonium sulfate (AS) or any combination thereof; Including, flowing a flue gas stream through or adjacent said at least one filter medium; wherein the flue gas stream comprises: Nitric oxide (NO), and Nitrogen dioxide (NO ２ ) Including NO ｘ a compound, the flue gas stream being at a first temperature during the flow process; The NO of the at least one filter medium ｘ Increasing the removal efficiency; Here, the NO of the at least one filter medium ｘ Increasing the removal efficiency means ammonia (NH) at a concentration in the range of 0.0001% to 0.5% of the concentration of said flue gas stream ３ ) and increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature. wherein the method regenerates the at least one filter medium.

2. The method of claim 1 , wherein the second temperature is 10° C. to 100° C. higher than the first temperature.

3. The method of claim 1, wherein the first temperature is in the range of 180°C to 230°C.

4. The method of claim 1, wherein the second temperature is in the range of at least 240°C to 280°C.

5. The method of claim 1 , wherein the flue gas flow is caused to flow across a cross-section of the at least one filter media such that the flue gas flow passes through a cross-section of the at least one filter media.

6. The method of claim 1 , wherein the flue gas flow is not passed across a cross-section of the at least one filter media such that the flue gas flow does not pass through a cross-section of the at least one filter media.

7. The method of claim 1 , wherein the flue gas stream is caused to flow perpendicular to a cross-section of the at least one filter media.

8. The method of claim 1 , wherein the flue gas stream is caused to flow parallel to a cross-section of the at least one filter media.

9. 2. The method of claim 1, wherein the at least one filter media is disposed within at least one filter bag, the at least one filter bag is contained within at least one filter bag housing, and the at least one catalytic material is in the form of catalytic particles.

10. The flue gas stream is oxygen (O ２ ), water (H ２ O), nitrogen (N ２ ), carbon monoxide (CO), sulfur dioxide (SO ２ ), sulfur trioxide (SO ３ ), one or more hydrocarbons, or any combination thereof.

11. NO ｘ The removal efficiency was calculated by the initial NO ｘ The method of claim 1 , further comprising increasing the first temperature of the flue gas stream to the second temperature to maintain an efficiency of at least 70%.

12. 10. The method of claim 1, wherein the at least one filter media comprises a porous guard layer and a porous catalyst layer, the porous catalyst layer comprising at least one catalytic material.

13. The method of claim 12 , wherein the porous protective layer comprises a microporous layer, the microporous layer comprising an expanded polytetrafluoroethylene (ePTFE) membrane.

14. The at least one catalytic material may be vanadium monoxide (VO), vanadium trioxide (V ２ O ３ ), vanadium dioxide (VO ２ ), vanadium pentoxide (V ２ O ５ ), tungsten trioxide (WO ３ ), molybdenum trioxide (MoO ３ ), titanium dioxide (TiO ２ ), silicon dioxide (SiO ２ ), aluminum trioxide (Al ２ O ３ ), manganese oxide (MnO ２ ), zeolite, or any combination thereof.

15. The method of claim 12 , wherein the at least one catalytic material is adhered to the filter media by at least one adhesive.

16. 16. The method of claim 15, wherein the at least one adhesive is selected from polytetrafluoroethylene (PTFE), fluorinated ethylene propylene (FEP), high molecular weight polyethylene (HMWPE), high molecular weight polypropylene (HMWPP), perfluoroalkoxyalkane (PFA), polyvinylidene fluoride (PVDF), polyvinylidene fluoride (THV), chlorofluoroethylene (CFE), or any combination thereof.

17. providing at least one filter medium; wherein the at least one filter medium comprises at least one catalytic material. flowing the flue gas flow across a cross-section of the at least one filter medium such that the flue gas flow 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: Nitric oxide (NO), and Nitrogen dioxide (NO ２ ), Including NO ｘ compound, Sulfur dioxide (SO ２ ), as well as Ammonia (NH ３ ), Including, wherein the flue gas stream is at a first temperature during a flow process; and A certain NO of the at least one filter medium ｘ Maintaining removal efficiency; wherein the at least one filter medium has a constant NO ｘ maintaining the removal efficiency includes increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature.

1. A method for scrubbing a flue gas stream, comprising:

18. At least during the flow process, the SO ２ , N.H. ３ and NO ｘ The compound is present in an amount of 1 mg / m based on the total volume of the flue gas stream. ３ The method of claim 17, wherein the compound is present in an amount of

19. providing at least one filter medium; wherein the at least one filter medium comprises at least one catalytic material. flowing the flue gas stream adjacent a cross-section of the at least one filter medium such that the flue gas stream flows parallel to 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: Nitric oxide (NO), and Nitrogen dioxide (NO ２ ), Including NO ｘ compound, Sulfur dioxide (SO ２ ), as well as Ammonia (NH ３ ), Including, wherein the flue gas stream is at a first temperature during a flow process. A certain NO of the at least one filter medium ｘ Maintaining removal efficiency; wherein the at least one filter medium has a constant NO ｘ maintaining the removal efficiency includes increasing a temperature of the flue gas stream from the first temperature to a second temperature greater than the first temperature.

1. A method for scrubbing a flue gas stream, comprising:

20. providing at least one filter medium; wherein the at least one filter medium comprises at least one catalytic material. flowing the flue gas flow across a cross-section of the at least one filter medium such that the flue gas flow 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: Nitric oxide (NO), and Nitrogen dioxide (NO ２ ), Including NO ｘ compound, Sulfur dioxide (SO ２ ), as well as Ammonia (NH ３ ), Including, wherein the flue gas stream is at a first temperature during a flow process. The at least one filter medium is provided with a filter member having a first temperature and a second temperature, the second temperature being greater than the first temperature. ｘ The removal efficiency was calculated by the initial NO ｘ maintain at least 70% of its efficiency; 1. A method for scrubbing a flue gas stream, comprising:

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