System and process for removal of pollutants from a gas stream

• US 20020168302A1
• Filed: 07/31/2001
• Published: 11/14/2002
• Est. Priority Date: 08/01/2000
• Status: Active Grant

• Current Assignee: Enviroscrub Technologies Corp.
• Original Assignee: Enviroscrub Technologies Corp.
• Inventors: Hammel, Charles F., Boren, Richard M., Larson, Joshua E., Axen, Steve G., Kronbeck, Kevin P., Tuzinski, Patrick A., Huff, Ray V., Carlton, Steve C., Pahlman, Kathleen S., Pahlman, John E.
• Granted Patent: US 6,610,263 B2
• Time in Patent Office: Days
• US Class Current: 422/171
• CPC Class Codes: B01D 2253/10 Inorganic adsorbents
• CPC Class Codes: B01D 2253/112 Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
• CPC Class Codes: B01D 2253/304 Linear dimensions, e.g. particle shape, diameter
• CPC Class Codes: B01D 2253/306 Surface area, e.g. BET-specific surface
• CPC Class Codes: B01D 2257/302 Sulfur oxides
• CPC Class Codes: B01D 2257/304 Hydrogen sulfide
• CPC Class Codes: B01D 2257/404 Nitrogen oxides other than dinitrogen oxide
• CPC Class Codes: B01D 2257/602 Mercury or mercury compounds
• CPC Class Codes: B01D 2258/00 Sources of waste gases
• CPC Class Codes: B01D 2259/40 Further details for adsorption processes and devices
• CPC Class Codes: B01D 2259/41 using plural beds of the same adsorbent in series
• CPC Class Codes: B01D 53/04 with stationary adsorbents B01D53/025 takes precedence
• CPC Class Codes: B01D 53/0423 Beds in columns
• CPC Class Codes: B01D 53/0446 Means for feeding or distributing gases
• CPC Class Codes: B01D 53/0454 Controlling adsorption controlling temperature swing adsorption B01D53/0462, controlling pressure swing adsorption B01D53/047
• CPC Class Codes: B01D 53/06 with moving adsorbents, e.g. rotating beds B01D53/025 takes precedence
• CPC Class Codes: B01D 53/08 according to the "moving bed" method
• CPC Class Codes: B01D 53/12 according to the "fluidised technique"
• CPC Class Codes: B01D 53/30 Controlling by gas-analysis apparatus regulating non electrical variables in general G05D
• CPC Class Codes: B01D 53/346 Controlling the process
• CPC Class Codes: B01D 53/508 : by treating the gases with solids
• CPC Class Codes: B01D 53/565 : by treating the gases with solids
• CPC Class Codes: B01D 53/60 : Simultaneously removing sulfur oxides and nitrogen oxides
• CPC Class Codes: B01D 53/64 : Heavy metals or compounds thereof, e.g. mercury
• CPC Class Codes: B01D 53/83 : with moving reactants
• CPC Class Codes: B01D 53/8609 : Sulfur oxides
• CPC Class Codes: B01D 53/8628 : Processes characterised by a specific catalyst
• CPC Class Codes: B01D 53/8665 : Removing heavy metals or compounds thereof, e.g. mercury
• CPC Class Codes: B01J 23/34 : Manganese
• CPC Class Codes: B01J 23/92 : of catalysts comprising metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
• CPC Class Codes: B01J 35/40 : characterised by dimensions, e.g. grain size in a colloidal state B01J35/23; crystallite size B01J35/77
• CPC Class Codes: C22B 43/00 : Obtaining mercury
• CPC Class Codes: C22B 7/006 : Wet processes
• CPC Class Codes: C22B 7/02 : Working-up flue dust
• CPC Class Codes: F23J 15/006 : Layout of treatment plant
• CPC Class Codes: F23J 15/02 : of purifiers, e.g. for removing noxious material traps for solid residues F23J3/04
• CPC Class Codes: F23J 2215/10 : Nitrogen; Compounds thereof
• CPC Class Codes: F23J 2215/20 : Sulfur; Compounds thereof
• CPC Class Codes: F23J 2215/60 : Heavy metals; Compounds thereof
• CPC Class Codes: F23J 2217/101 : Baghouse type
• CPC Class Codes: F23J 2219/60 : Sorption with dry devices, e.g. beds
• CPC Class Codes: G05D 16/028 : Controlling a pressure difference control of flow G05D7/00
• CPC Class Codes: G05D 16/2013 : using throttling means as controlling means
• CPC Class Codes: G05D 21/02 : characterised by the use of electric means
• CPC Class Codes: G05D 23/1917 : using digital means
• CPC Class Codes: G05D 7/0635 : by action on throttling means G05D7/0688, G05D7/0694 take precedence
• CPC Class Codes: Y02C 20/10 : of nitrous oxide (N2O)
• CPC Class Codes: Y02P 10/122 : by capturing or storing CO2
• CPC Class Codes: Y02P 10/146 : Perfluorocarbons [PFC]; Hydrofluorocarbons [HFC]; Sulfur hexafluoride [SF6]
• CPC Class Codes: Y02P 10/20 : Recycling
• CPC Class Codes: Y10S 423/05 : Automatic, including computer, control

Abstract

System for removal of targeted pollutants, such as oxides of sulfur, oxides of nitrogen, mercury compounds and ash, from combustion and other industrial process gases and processes utilizing the system. Oxides of manganese are utilized as the primary sorbent in the system for removal or capture of pollutants. The oxides of manganese are introduced from feeders into reaction zones of the system where they are contacted with a gas from which pollutants are to be removed. With respect to pollutant removal, the sorbent may interact with a pollutant as a catalyst, reactant, adsorbent or absorbent. Removal may occur in single-stage, dual-stage, or multi-stage systems with a variety of different configurations and reaction zones, e.g., bag house, cyclones, fluidized beds, and the like. Process parameters, particularly system differential pressure, are controlled by electronic controls to maintain minimal system differential pressure, and to monitor and adjust pollutant removal efficiencies. Reacted sorbent may be removed from the reaction action zones for recycling or recycled or regenerated with useful and marketable by-products being recovered during regeneration.

Claims

1. An adaptable system for dry removal of oxides of sulfur (SO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A reaction zone configured for introduction of the sorbent and a gas containing SO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the reaction zone being further configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted sorbent so that the gas may be vented from the reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

4. A system according to any one of claims 1-3, further comprising a section of pipe/duct acting as a reaction zone connected to an inlet of another reaction zone, the section of pipe/duct being configured for introduction and commingling of the gas and sorbent for sufficient amount of time to effect a reaction.

5. A system according to any one of claims 1-3, wherein the reaction zone is selected from the group consisting of a fluidized bed, a pseudo-fluidized bed, a reaction column, a fixed bed, a pipe/duct reactor, a moving bed, a bag house, an inverted bag house, bag house reactor, serpentine reactor, and a cyclone/multiclone.

27. An adaptable system according to any one of claims 1-3, wherein the reaction zone includes a filter having a sorbent filter cake having a bed thickness formed thereupon, further comprising a feedback pollutant controller for controlling the output level of pollutant gases, wherein the pollutant gases are selected from the group consisting of NO, NO₂, N₂O, N₂O₃, SO₂, and SO₃ and combinations thereof, and a controller input signal indicative of the pollutant level, and a controller output controlling the overall filter cake thickness in the reaction zone, wherein the pollutant controller decreases the filter cake thickness to increase the pollutant level and increases the filer cake thickness to decrease the pollutant level.

30. An adaptable system according to any one of claims 1-3, further comprising a pollutant sensor for measuring the SO_X or NO_X level downstream of the reaction zone, a pollutant controller for controlling the pollutant level downstream of the reaction zone, wherein the pollutant controller is a feed back controller accepting a pollutant level set point and outputting a signal to control the sorbent feeder rate, wherein the controller increases the feed rate signal to decrease the pollutant level and decreases the feed rate signal to increase the pollutant level.

31. An adaptable system according to any one of claims 1-3, further comprising a reaction zone outlet temperature sensor, further comprising reaction zone temperature feed back controller for controlling the reaction zone temperature, wherein the temperature controller accepts a set point, wherein the controller increases the reaction zone temperature in response to a reaction zone temperature less than the set point and decreases the reaction zone temperature in response to a reaction zone temperature greater than the set point.

32. An adaptable system according to any one of claims 1-3 and 6-26, wherein at least one reaction zone is a bag house reactor having a variable venturi and wherein the system further comprises a controller for monitoring and adjusting the position of the variable venturi by detecting the position of the variable venturi, comparing the position of the variable venturi against a variable venturi position set point, and adjusting the position of the variable venturi to attempt to match the variable venturi set point.

33. An adaptable system according to any one of claims 1-3 and 6-26, wherein at least one reaction zone is a bag house, wherein the bag house is comprised of a plurality of fabric filters and a plurality of pulse valves for cleaning the filters, wherein the pulse valves accept a pulse signal to clean at least one filter, further comprising a differential pressure sensor for measuring the differential pressure across the bag house, wherein the system further comprises a feedback controller for monitoring and adjusting the differential pressure across the bag house, wherein the differential pressure controller inputs the measured differential pressure and accepts a differential pressure set point and generates an output signal to at least one pulse valve, wherein the differential pressure controller increases the frequency of pulse valve output signals in response to a differential pressure higher than set point and decreases the frequency of pulse valve output signals in response to a differential pressure lower than set point.

36. An adaptable system according to any one of claims 1-3 and 6-26, further comprising a controller for monitoring and adjusting the position of a variable venturi mounted within a bag house, thereby controlling the depth of the pseudo fluidized bed, the controller comprised of a variable venturi position controller that measures and adjusts the position of the variable venturi, input/output modules mounted on nodes, and a PID loop which electronically communicates with the position controller through the input/output modules and nodes, the PIED loop being programmed with a targeted variable venturi position set point and further programmed to read and compare variable venturi position measurements against targeted variable venturi position set point and to signal the variable venturi position controller to vary the variable venturi position to comparing the position of the variable venturi against variable venturi position set points, and adjusting the position of the variable venturi to reconcile with targeted variable venturi set points.

37. An adaptable system according to any one of claims 1-3 and 6-26, further comprising a controller for simultaneous monitoring and adjusting of SO_X capture rate, NO_X capture rate, and system differential pressure based upon maximum error signal for these operational parameters, the controller being comprised of a plurality of fabric filter bag pulse valves for cleaning sorbent from the filter bags, a bag house differential pressure controller which measures and controls the pulse rate of the pulse valves, continuous emissions monitors for measuring SO_X and/or NO_X concentrations in an inlet gas and an outlet gas, feeder rate controller for increasing and decreasing the sorbent feeder rate, input/output modules mounted on nodes, an error gate, a gain selector in electronic communication with a fixed database having SO_X gains, NO_X gains and differential pressure gains entered therein, a selector gate in electronic communication with a fixed database having NO_X set points, SO_X set points and differential pressure set points entered therein, an error generator in electronic communication with the differential pressure controller and the continuous emissions monitors, the error generator being programmed to read and compare differential pressure measurements against the set points and to generate error signals that are filtered through the error gate selector, a PID loop in electronic communication with the gain selector, the selector gate, the error gate, the feed rate controller, and the differential pressure controller through the input/output modules and nodes, the PID loop being programmed to read the error signal filtered through the error gate, to subtract the error signals for NO_X capture rate(s), SO_X capture rate(s) and differential pressure from their respective targeted set points, to the compare the results to determine the operating parameter with the maximum error signal, and to signal the differential pressure controller to increase or decrease the pulse rate of the plurality of pulse valves to adjust system differential pressure to reconcile differential pressure with targeted differential pressure set point, if maximum error signal is for differential pressure, to signal the feeder rate controller to increase or decrease sorbent feeder rate to increase or decrease the rate of NO_X or SO_X capture to adjust the capture rate to reconcile with targeted SO_X or NO_X capture rate set points, if the maximum error signal is for NO_X or SO_X capture rate. To adjust the capture rate for NO_X or SO_X to reconcile, if the maximum error signal is for NO_X or SO_X capture rate.

38. An adaptable system according to any one of claims 1-3 and 6-26, further comprising a control system for simultaneous monitoring and adjusting NO_X and or SO_X capture rates, system differential pressure, and gas inlet temperature.

39. An adaptable system according to any one of claims 1-3 and 6-26, further comprising a control system for simultaneous monitoring and adjusting NO_X and or SO_X capture rates, system differential pressure, gas inlet temperature, and variable venturi position.

44. The system of any one of claims 1-3 and 6-26, wherein the system further comprises a reacted sorbent feeder for recycling reacted sorbent to the reaction zone of the system.

48. The system of any one of claims 1-3 and 6-26 wherein the system further comprises at least one sorbent preheater for preheating of sorbent.

77. A process for dry removal of oxides of sulfur as in claim 49, wherein the reaction zone includes a filter, wherein the contacting step includes contacting the gas containing SO_X with a filter cake of the sorbent formed on the filter, wherein the process further includes providing a differential pressure controller for controlling the differential pressure across the filter, wherein the differential pressure controller includes a set point, an input indicative of the differential pressure, and an output to control the cleaning rate of the filter cake, wherein the method includes using the differential pressure controller to control the differential pressure to match the set point by increasing the cleaning rate to decrease the differential pressure and by decreasing the cleaning rate to increase the differential pressure.

78. A process for dry removal of oxides of sulfur as in claim 77, wherein the process further includes providing an outlet SO_X sensor for measuring an outlet gas SO_X level downstream of the filter, providing a SO_X level controller for controlling the SO_X level downstream of the filter, wherein the SO_X level controller includes a set point, an input indicative of the outlet SO_X level, and an output to control the cleaning rate of the filter cake, wherein the method includes using the controller to control the SO_X level to match the set point by increasing the cleaning rate to increase the outlet SO_X level by decreasing the thickness of the filter cake bed depth, and by decreasing the cleaning rate to decrease the outlet SO_X level by increasing the thickness of the filter cake.

79. A process for dry removal of oxides of sulfur as in claim 78, wherein the SO_X level controller output operates upon the set point of a filter differential pressure controller.

80. A process for dry removal of oxides of sulfur as in claim 49, wherein the process further includes providing an outlet SO_X sensor for measuring an outlet gas SO_X level downstream of the filter, providing a SO_X level controller for controlling the SO_X level downstream of the filter, wherein the SO_X level controller includes a set point, an input indicative of the outlet SO_X level, and an output to control the temperature of the reaction zone, wherein the method includes using the controller to control the SO_X level to match the set point by increasing the reaction zone temperature to increase the outlet SO_X level, and by decreasing the reaction zone temperature to decrease the outlet SO_X level.

81. A process for dry removal of oxides of sulfur as in claim 49, wherein the filter includes a plurality of subfilters, and the cleaning rate control includes controlling the cleaning frequency of the subfilters.

82. A process for dry removal of oxides of sulfur as in claim 49, wherein the introducing sorbent step includes injecting the sorbent into the gas at a controllable sorbent feed rate, wherein the process further includes providing an outlet SO_X sensor for measuring an outlet gas SO_X level downstream of the reaction zone, providing a SO_X level controller for controlling the SO_X level downstream of the reaction zone, wherein the SO_X level controller includes a set point, an input indicative of the outlet SO_X level, and an output to control the sorbent feed rate to the reaction zone, wherein the process includes using the controller to control the SO_X level to match the set point by decreasing the sorbent feed rate to increase the outlet SO_X level, and by increasing the sorbent feed rate to decrease the outlet SO_X level.

2. An adaptable system for dry removal of oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A reaction zone configured for introduction of the sorbent and a gas containing NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, the reaction zone being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

3. An adaptable system for dry removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A reaction zone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

34. An adaptable system according to claim 3, further comprising a SO_X sensor for measuring the SO_X level downstream of the reaction zone, a NO_X sensor for measuring the NO_X level downstream of the reaction zone, a pollutant controller for controlling the pollutant level downstream of the reaction zone, wherein the pollutant controller is a feedback controller, wherein the pollutant controller generates a signal to the sorbent feeder to control the sorbent feeder rate, the system further comprising a selector, wherein the selector accepts a S O_X set point and accepts the SO_X level from the SO_X sensor, and generates a SO_X deviation signal indicative of the deviation between the SO_X level and the SO_X set point, wherein the selector accepts a NO_X set point, accepts the NO_X level from the NO_X sensor, and generates a NO_X deviation signal indicative of the deviation between the NO_X level and the NO_X set point, wherein the selector compares the magnitude of the SO_X deviation and the NO_X deviation, and determines the larger magnitude deviation for output, such that the pollutant controller controls the sorbent feeder based on the SO_X or NO_X level having the greatest deviation from set point, wherein the controller increases the sorbent feeder rate signal to decrease the pollutant level and decreases then sorbent feed rate signal to increase the pollutant level.

6. An adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first reaction zone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

c. A second reaction zone configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the first reaction zone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

7. A adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

b. A modular reaction unit comprised of at least three (3) interconnected reaction zones, the reaction zones being connected so that a gas containing SO_X and/or NO_X can be routed through any one of the reaction zones, any two of the reaction zones in series, or all of the at least three reaction zones in series or in parallel, or any combination of series and parallel, each reaction zone being separately connected to the feeder so that sorbent can be introduced into each reaction zone where SO_X and/or NO_X capture can occur when the gas is contacted with sorbent for a time sufficient to allow formation of sulfates of manganese, nitrates of manganese, or both; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

8. A adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

b. A modular reaction unit comprised of at least three (3) interconnected bag houses, the bag houses being connected so that a gas containing SO_X and/or NO_X can be routed through any one of the bag houses, any two of the bag houses in series, or all of the at least three bag houses in series or in parallel, or any combination of series and parallel, each bag house being separately connected to the feeder so that sorbent can be introduced into each bag house where SO_X and/or NO_X capture can occur when the gas is contacted with sorbent for a time sufficient to allow formation of sulfates of manganese, nitrates of manganese, or both; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

9. An adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

b. A modular reaction unit comprised of at least three (3) interconnected reaction zones, the reaction zones being connected so that a gas containing SO_X and/or NO_X can be routed through any one of the reaction zones, any two of the reaction zones in series, or all of the at least three reaction zones in series or in parallel, or any combination of series and parallel, each reaction zone being separately connected to the feeder so that sorbent can be introduced into each reaction zone where SO_X and/or NO_X capture can occur when the gas is contacted with sorbent for a time sufficient to allow formation of sulfates of manganese, nitrates of manganese, or both, with SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, the reaction zones each being configured to render the gas that has been substantially stripped of SO_X and/or NO_X free of reacted and unreacted sorbent so that the gas that has been substantially stripped of SO_X and/or NO_X may be vented from the reaction zones or passed from one reaction zone to another reaction zone in series; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

10. An adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

b. A modular reaction unit comprised of at least three (3) interconnected bag houses, the bag houses being connected so that a gas containing SO_X and/or NO_X can be routed through any one of the bag houses, any two of the bag houses in series, or all of the at least three bag houses in series or in parallel, or any combination of series and parallel, each bag house being separately connected to the feeder so that sorbent can be introduced into each bag house where SO_X and/or NO_X capture can occur when the gas is contacted with sorbent for a time sufficient to allow formation of sulfates of manganese, nitrates of manganese, or both, with SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, the bag houses each being configured to render the gas that has been substantially stripped of SO_X and/or NO_X free of reacted and unreacted sorbent so that the gas that has been substantially stripped of SO_X and/or NO_X may be vented from the bag houses or passed from one bag house to another bag house in series; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

11. An adaptable system for removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first reaction zone configured for introduction of sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X;

the first reaction zone being configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted absorbent so that the gas can be directed out of the first reaction zone free of reacted and unreacted absorbent;

c. A second reaction zone and a third reaction zone each connected to the first reaction zone by a common conduit, where the gas that has been substantially stripped of SO_X in the first reaction zone is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second and third reaction zones each being configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second and third reaction zones free of reacted and unreacted sorbent; and

d. A diverter valve positioned in the common conduit so as to direct the flow of gas from the first reaction zone to the second reaction zone and/or the third reaction zone, the diverter valve having variable positions, in one position gas from the first reaction zone is directed to the second reaction zone, in another position gas from the first reaction zone is directed to both the second and third reaction zones, and in a further position gas from the first reaction zone is directed to the third reaction zone;

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

45. The system of any one of claims 6, 7, 9, 11, 19, and 24, wherein the system further comprises a reacted sorbent feeder for recycling reacted sorbent from the second reaction zone to the first reaction zone.

46. The system of any one of claims 6, 7, 9, 11, 19, and 24, wherein the system further comprises a first reacted sorbent feeder for recycling reacted sorbent from the first reaction zone for re-introduction into the first reaction zone and a second reacted sorbent feeder for recycling reacted sorbent from the second reaction zone for re-introduction into the second reaction zone.

47. The system of any one of claims 6, 7, 9, 11, 19, and 24, wherein the system further comprises a reacted sorbent feeder for receiving reacted sorbent from the second reaction zone, with reacted sorbent from the reacted sorbent feed being introduced into the first reaction zone.

12. An adaptable system for removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first bag house configured for introduction of sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X;

the first bag house being configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted absorbent so that the gas can be directed out of the first bag house free of reacted and unreacted absorbent;

c. A second bag house and a third bag house each connected to the first bag house by a common conduit, where the gas that has been substantially stripped of SO_X in the first bag house is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second and third bag houses each being configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second and third bag houses free of reacted and unreacted sorbent; and

d. A diverter valve positioned in the common conduit so as to direct the flow of gas from the first bag house to the second bag house and/or the third bag house, the diverter valve having variable positions, in one position gas from the first bag house is directed to the second bag house, in another position gas from the first bag house is directed to both the second and third bag houses, and in a further position gas from the first bag house is directed to the third bag house;

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

40. A system according to any one of claims 6, 7, 9, 12, 17, 19, 22, and 24 wherein a reaction zone is selected from the group consisting of a fluidized bed, a pseudo-fluidized bed, a reaction column, a fixed bed, a pipe/duct reactor, a moving bed, a bag house, an inverted bag house, bag house reactor, serpentine reactor, and a cyclone/multiclone.

13. An adaptable system for removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. At least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first bag house configured for introduction of sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X;

the first bag house being configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted absorbent so that the gas can be directed out of the first bag house free of reacted and unreacted absorbent;

c. A second bag house and a third bag house each connected to the first bag house by a common conduit, where the gas that has been substantially stripped of SO_X in the first bag house is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second and third bag houses each being configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second and third bag houses free of reacted and unreacted sorbent;

d. A diverter valve positioned in the common conduit so as to direct the flow of gas from the first bag house to the second bag house and/or the third bag house, the diverter valve having variable positions, in one position gas from the first bag house is directed to the second bag house, in another position gas from the first bag house is directed to both the second and third bag houses, and in a further position gas from the first bag house is directed to the third bag house; and

e. At least one off-line loading circuit for pre-loading of sorbent onto fabric filter bags mounted within the second and third bag houses when the bag houses are off-line, the off-line loading circuit being comprised of;

i. An off-line loading circuit conduit configured for introduction of sorbent, the loading circuit conduit having a first end and a second end, the first end being connected to the feeder and the second end being connected to the bag houses;

ii. A recirculation fan for blowing air and sorbent into each of the second and

third bag houses to pre-load sorbent onto the filter fabric bags mounted therein;

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

14. An adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first bag house configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

c. A second bag house zone configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the first reaction zone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

15. An adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A cyclone/multiclone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

c. A bag house configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the cyclone/multiclone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

16. An adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A serpentine reactor configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

c. A bag house configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the section of serpentine pipe/duct where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

17. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. At least one reaction zone configured for introduction of the sorbent and the gas containing SO_X, NO_X, mercury compounds, and ash where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decompostion temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by adsorption onto the sorbent, the reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent, mercury compounds, and ash so that the gas may be vented from the reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

18. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. At least one bag house configured for introduction of the sorbent and the gas containing SO_X, NO_X, mercury compounds, and ash where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decompostion temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by adsorption onto the sorbent, the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent, mercury compounds, and ash so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

19. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1100 m²/g;

b. A first reaction zone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by adsorption onto the sorbent to substantially strip the gas of mercury compounds, the first reaction zone being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury compounds, and ash so that the gas may be vented from the first reaction zone; and

c. A second reaction zone configured for introduction of sorbent and the gas vented from the first reaction zone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second reaction zone being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

20. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first bag house configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by adsorption onto the sorbent to substantially strip the gas of mercury compounds, the first bag house being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury compounds, and ash so that the gas may be vented from the first bag house; and

c. A second bag house configured for introduction of sorbent and the gas vented from the first bag house where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

21. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A cyclone/multiclone configured for introduction of the sorbent and a gas containing SO_X, NO_X, mercury compounds and ash, where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by adsorption onto the sorbent to substantially strip the gas of mercury compounds, the cyclone/multiclone being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury compounds, and ash so that the gas may be vented from the cyclone/multiclone; and

c. A bag house configured for introduction of sorbent and the gas vented from the cyclone/multiclone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

22. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, elemental mercury vapor, and ash from gases with minimal differential pressure across the system, comprising:

a. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. at least one reaction zone configured for introduction of the sorbent and the gas containing SO_X, NO_X, mercury compounds, mercury vapor, and ash where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decompostion temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by adsorption onto the sorbent, the reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent, mercury compounds, mercury vapor, and ash so that the gas may be vented from the reaction zone; and

c. A mercury-alumina reactor configured for introduction of the gas vented from the reaction zone and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface(s) of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury compounds in the gas, the mercury being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been partially substantially stripped of mercury vapor free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

28. An adaptable system according to claim 27, wherein the pollutant controller controls the cleaning rate of the filters.

29. An adaptable system according to claim 27, further comprising a feedback differential pressure controller for controlling the differential pressure across the reaction zone, and a controller input signal indicative of the differential pressure across the reaction zone, and a controller output controlling the overall filter cake thickness in the reaction zone, wherein the differential pressure controller decreases the filter cake thickness to decrease the differential pressure and increases the filer cake depth to increase the differential pressure.

35. An adaptable system according to claim 29, wherein the differential pressure controller controls the cleaning rate of filters in the reaction zone.

23. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, elemental mercury vapor, and ash from gases with minimal differential pressure across the system, comprising:

a. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. at least one bag house configured for introduction of the sorbent and the gas containing SO_X, NO_X, mercury compounds, mercury vapor, and ash where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decompostion temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by reacting mercury vapor with the sorbent to form mercury oxide(s) which along with mercury compounds are captured by absorption onto the sorbent, the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent, mercury compounds, mercury vapor, and ash so that the gas may be vented from the bag house; and

c. A mercury-alumina reactor configured for introduction of the gas vented from the bag house and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface(s) of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury compounds in the gas, the mercury being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been partially substantially stripped of mercury vapor free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

24. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, mercury vapor, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first reaction zone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by absorption onto the sorbent to substantially strip the gas of mercury compounds, the first reaction zone being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury oxide, salts of mercury, and ash so that the gas may be vented from the first reaction zone;

c. A second reaction zone configured for introduction of sorbent and the gas vented from the first reaction zone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second reaction zone being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second reaction zone; and

d. An alumina reactor configured for introduction of the gas vented from the second reaction zone and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface(s) of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury compounds in the gas, the mercury being capture by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been substantially stripped of mercury compounds free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

25. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, mercury vapor, and ash from gases with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A first bag house configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by adsorption onto the sorbent to substantially strip the gas of mercury compounds, the first bag house being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, and ash so that the gas may be vented from the first bag house;

c. A second bag house configured for introduction of sorbent and the gas vented from the first bag house where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second bag house; and

d. A mercury-alumina reactor configured for introduction of the gas vented from the second bag house and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface(s) of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury compounds in the gas, the mercury being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been substantially stripped of mercury compounds free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

26. An adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in particulate form, mercury vapor, and ash from gas with minimal differential pressure across the system, comprising:

a. A feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

b. A cyclone/multiclone configured for introduction of the sorbent and a gas containing SO_X, NO_X, mercury compounds, mercury vapor and ash, where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by adsorption onto the sorbent to substantially strip the gas of mercury compounds, the cyclone/multiclone being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, and ash so that the gas may be vented from the cyclone/multiclone;

c. A bag house configured for introduction of sorbent and the gas vented from the cyclone/multiclone where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

d. An alumina reactor configured for introduction of the gas vented from the second bag house and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface(s) of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury compounds in the gas, the mercury being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been partially substantially stripped of mercury compounds free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

41. An inverted bag house permitting downward vertical flow of gases and sorbent, comprised of;

a. A bag house housing which permits the introduction of gases and sorbent entrained in the gases, the housing having a top and a bottom and being configured for gases to flow vertically downward from the top to the bottom of the bag house;

b. At least one inlet at the top of the housing, the inlet being located near the top of the bag house housing and configured for the introduction of gases and sorbent entrained in the gases into the bag house;

c. A plurality of fabric filter bags configured to allow gas to flow from the outside of the bags to the inside of the bags under an applied differential pressure and to prevent the passage of sorbent from the outside to the inside of the bags, thereby separating sorbent from the gas;

d. A support structure for receiving and supporting the plurality of fabric filter bags, the support structure being configured to receive and support the fabric filter bags and to provide openings through which particles may be freely passed downward into the hopper by gravity;

e. A hopper to receive and collect the particles that pass downward through the openings of the frame and from which the particles may be removed, the hopper being configured to permit the removal of the particles;

f. An outlet located near the bottom of the housing below the bags and above the hopper;

g. A conduit located below the fabric filter bags and positioned to receive gas passing through the fabric filter bags the conduit being in flow-through connection with the outlet.

42. A bag house reactor for removal of pollutants from a gas stream by contacting the gas with a sorbent and separation of sorbent that are entrained in the gas, comprising:

a. a bag house having a housing with interior and exterior surfaces, and upper, central, and lower sections;

b. a variable venturi for adjusting the velocity of gas flowing though the venturi, thereby controlling depth of the pseudo-fluidized bed, the variable venturi being generally located in the central and/or lower sections of the bag house and configured for the adjustment of the position of the variable venturi by varying the distance between the variable venturi and the interior surface of the bag house and having a variable venturi position detector for determining the position of the variable venturi and a variable venturi positioner for adjusting the position of the variable venturi to increase or decrease the velocity of gas flow from the lower section past the variable venturi to the central and upper sections of the bag house;

c. a gas distribution conduit configured for introduction of gas, the first gas distribution port being positioned below the variable venturi,

d. a sorbent port connected to a sorbent feeder conduit configured for introduction of sorbent into the bag house, the sorbent distribution port being positioned above the variable venturi,

e. a plurality of fabric filter bags secured therein, the fabric filter bags being mounted in the upper section of the bag house and extending downward into the central section,

f. a sorbent hopper located in the bottom section of the bag house where loaded sorbent is collected,

g. a reacted sorbent outlet being connected to the sorbent hopper and having an outlet valve which in the open position allows for removal of sorbent from the hopper; and

h. a vent located in the top section of the bag house for venting of gas from the bag house.

43. An adaptable system for dry removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising:

a. a bag house reactor for removal of pollutants from gases by contacting the gas with a sorbent and separation of the sorbent particles that are entrained in the gas, the bag house reactor being comprised of;

i. a bag house having a housing with interior and exterior surfaces, and upper, central, and lower sections;

ii. a variable venturi for adjusting the velocity of gas flowing though the venturi, thereby controlling depth of the pseudo-fluidized bed, the variable venturi being generally located in the central and/or lower sections of the bag house and configured for the adjustment of the position of the variable venturi by varying the distance between the variable venturi and the interior surface of the bag house and having a variable venturi position detector for determining the position of the variable venturi and a variable venturi positioner for adjusting the position of the variable venturi to increase or decrease the velocity of gas flow from the lower section past the variable venturi to the central and upper sections of the bag house;

iii. a gas distribution port connected to a conduit configured for introduction of gas into the bag house, the gas distribution port being positioned below the variable venturi,

iv. a sorbent distribution port connected to a sorbent feeder conduit configured for introduction of sorbent into the bag house, the sorbent distribution port being positioned above the variable venturi,

v. a plurality of fabric filter bags secured therein, the fabric filter bags being mounted in the upper section of the bag house and extending downward into the central section,

vi. a sorbent hopper located in the bottom section of the bag house where loaded sorbent is collected,

vii. aloaded sorbent outletbeing connected to the sorbent hopper and having an outlet valve which in the open position allows for removal of sorbent from the hopper; and

viii. a vent located in the top section of the bag house for venting of gas from the bag house; and

b. a sorbent feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size of less than about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g, the sorbent feeder being connected to the sorbent feeder conduit and being further configured to introduce sorbent into the first sorbent feeder conduit; and

wherein the system is regulated so that differential pressure across the system is no greater than a predetermined level.

49. A process for dry removal of oxides of sulfur (SO_X) from a gas stream, comprising the step of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) from gases with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

ii. a reaction zone configured for introduction of the sorbent and a gas containing SO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the reaction zone being further configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted sorbent so that the gas may be vented from the reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X into the reaction zone, the gas being at temperatures typically ranging from ambient temperature to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture set point through the formation of sulfates of manganese to substantially strip the gas of SO_X thereby reacting with the sorbent;

D. rendering the gas free of reacted and unreacted sorbent;

E. venting the gas from the reaction zone.

66. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system;

washing the sorbent in a dilute acid rinse to dissolve sulfates and/or nitrates of manganese on the surface of sorbent particles into solution and thereby cleaning the sorbent;

separating the cleaned sorbent from the acid rinse;

drying the cleaned sorbent; and

pulverizing the cleaned sorbent to de-agglomerate the cleaned sorbent.

67. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system;

washing the sorbent in a dilute acid rinse to dissolve sulfates and/or nitrates of manganese on the surface of sorbent particles into solution and thereby cleaning the sorbent;

separating the cleaned sorbent from the acid rinse;

conveying the cleaned sorbent to a dryer;

drying the cleaned sorbent;

conveying the cleaned sorbent to a pulverizer;

pulverizing the cleaned sorbent to de-agglomerate the cleaned sorbent; and

conveying the de-agglomerated clean sorbent to the sorbent feeder for reintroduction into the system.

68. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system;

washing the sorbent in a dilute acid rinse to dissolve sulfates and/or nitrates of manganese on the surface of sorbent particles into solution and thereby cleaning the sorbent;

separating the cleaned sorbent from the acid rinse to provide a filtrate containing dissolved sulfates and/or nitrates of manganese;

adding alkali or ammonium hydroxide to the filtrate to form an unreacted sorbent precipitate of oxides and hydroxides of manganese and a liquor containing alkali or ammonium sulfates and/or nitrates;

separating the unreacted sorbent precipitate from the liquor, the liquor being routed for further processing into marketable products or for distribution and/or sale as a useful by-product;

rinsing the sorbent precipitate;

drying the sorbent precipitate to form unreacted sorbent; and

pulverizing the unreacted sorbent to de-agglomerate the unreacted sorbent.

69. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system;

washing the sorbent in a dilute acid rinse to dissolve sulfates and/or nitrates of manganese on the surface of sorbent particles into solution and thereby cleaning the sorbent;

separating the cleaned sorbent from the acid rinse to provide a filtrate containing dissolved sulfates and/or nitrates of manganese;

adding alkali or ammonium hydroxide to the filtrate to form a sorbent precipitate of oxides of manganese and a liquor containing alkali or ammonium sulfates and/or nitrates;

separating the sorbent precipitate from the liquor, the sorbent precipitate being routed for regeneration of unreacted sorbent; and

routing the liquor for distribution and/or sale as a useful by-product or for further processing into marketable products.

70. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system where primarily NO_X capture occurred by reacting with the sorbent to form nitrates of manganese;

heating the reacted sorbent to thermally decompose the nitrates of manganese, to desorb NO₂, and to regenerate reacted sorbent to form unreacted sorbent of oxides of manganese; and

further heating the unreacted sorbent in an oxidizing atmosphere to complete the regeneration of the sorbent.

71. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system where primarily NO_X capture occurred by reacting with the sorbent to form nitrates of manganese;

heating the reacted sorbent to thermally decompose the nitrates of manganese, to desorb NO₂, and to regenerate reacted sorbent to form unreacted sorbent of oxides of manganese;

passing the desorbedNO₂ through a wet scrubber containing water and an oxidant to form a nitric acid liquor; and

routing the nitric acid liquor for further distribution and/or sale as a useful product or on for further processing.

72. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing reacted sorbent from a reaction zone of the system where primarily NO_X capture occurred by reacting with the sorbent to form nitrates of manganese;

heating the reacted sorbent to thermally decompose the nitrates of manganese, to desorbNO₂, and to regenerate reacted sorbent to form unreacted sorbent of oxides of manganese;

passing the desorbedNO₂ through a wet scrubber containing water and an oxidant to form a nitric acid liquor;

adding an ammonium or alkali hydroxide to the acid liquor to form a liquor containing ammonium or alkali nitrates; and

routing the liquor for distribution and/or sale as a useful by-product or for further processing into marketable products.

73. The process of any one of claims 49-65, wherein the process further comprises the steps of:

removing SO_X and NO_X reacted sorbent from a reaction zone of the system;

heating the reacted sorbent to a first temperature to desorb NO₂, the desorbed NO being routed for further processing and/or handling; and

heating the reacted sorbent to a second temperature to desorb SO_X, the desorbed SO_X being routed for further processing and/or handling and the reacted sorbent being regenerated to unreacted sorbent.

50. A process for dry removal of oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

ii. a reaction zone configured for introduction of the sorbent and a gas containing NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of nitrates of manganese and contacted with the sorbent for a time sufficient to effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, the reaction zone being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the reaction zone;

and wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing NO_X into the reaction zone, the gas being at temperatures typically ranging from ambient temperature to a temperature below the thermal decomposition temperature(s) of nitrates of manganese;

C. contacting the gas with sorbent for a time sufficient to effect NO_X capture at a targeted NO_X capture set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

D. rendering the gas free of reacted and unreacted sorbent;

E. venting the gas from the reaction zone.

83. A process for dry removal of oxides of nitrogen as in claim 50, wherein the reaction zone includes a filter, wherein the contacting step includes contacting the gas containing NO_X with a filter cake of the sorbent formed on the filter, wherein the process further includes providing a differential pressure controller for controlling the differential pressure across the filter, wherein the differential pressure controller includes a set point, an input indicative of the differential pressure, and an output to control the cleaning rate of the filter cake, wherein the method includes using the differential pressure controller to control the differential pressure to match the set point by increasing the cleaning rate to decrease the differential pressure and by decreasing the cleaning rate to increase the differential pressure.

84. A process for dry removal of oxides of nitrogen as in claim 83, wherein the process further includes providing an outlet NO_X sensor for measuring an outlet gas NO_X level downstream of the filter, providing a NO_X level controller for controlling the NO_X level downstream of the filter, wherein the NO_X level controller includes a set point, an input indicative of the outlet NO_X level, and an output to control the cleaning rate of the filter cake, wherein the method includes using the controller to control the NO_X level to match the set point by increasing the cleaning rate to increase the outlet NO_X level by decreasing the thickness of the filter cake, and by decreasing the cleaning rate to decrease the outlet NO_X level by increasing the thickness of the filter cake.

85. A process for dry removal of oxides of nitrogen as in claim 84, wherein the NO_X level controller output operates upon the set point of a filter differential pressure controller.

86. A process for dry removal of oxides of nitrogen as in claim 83, wherein the method further includes providing an outlet NO_X sensor for measuring an outlet flue gas NO_X level downstream of the filter, providing a NO_X level controller for controlling the NO_X level downstream of the filter, wherein the NO_X level controller includes a set point, an input indicative of the outlet NO_X level, and an output to control the temperature of the reaction zone, wherein the method includes using the controller to control the NO_X level to match the set point by increasing the reaction zone temperature to increase the outlet NO_X level, and by decreasing the reaction zone temperature to decrease the outlet NO_X level.

87. A process for dry removal of oxides of nitrogen as in claim 83, wherein the filter includes a plurality of subfilters, and the cleaning rate control includes controlling the cleaning frequency of the subfilters.

88. A process for dry removal of oxides of nitrogen as in claim 83, wherein the introducing sorbent step includes injecting the sorbent into the gas at a controllable sorbent feed rate, wherein the process further includes providing an outlet NO_X sensor for measuring an outlet gas NO_X level downstream of the reaction zone, providing a NO_X level controller for controlling the NO_X level downstream of the reaction zone wherein the NO_X level controller includes a set point, an input indicative of the outlet NO_X level, and an output to control the sorbent feed rate to the reaction zone, wherein the process includes using the controller to control the NO_X level to match the set point by decreasing the sorbent feed rate to increase the outlet NO_X level, and by increasing the sorbent feed rate to decrease the outlet NO_X level.

51. A process for dry removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a reaction zone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decompostion temperature(s) of nitrates of manganese and contacted with the sorbent for a time to sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and NO_X into the first reaction zone, the gas being at temperatures typically ranging from ambient temperature to a temperature below the thermal decomposition temperature(s) of nitrates of manganese;

C. contacting the gas with sorbent for a time sufficient to simultaneously effect SO_X capture at a targeted SO_X capture set point through the formation of sulfates of manganese to substantially strip the gas of SO_X and to effect NO_X capture at a targeted NO_X capture set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

D. rendering the gas free of reacted and unreacted sorbent;

E. venting the gas from the reaction zone.

52. A process for dry removal of SO_X and/or NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for dry removal (SO_X) and/or (NO_X) from gases with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a first reaction zone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

iii. a second reaction zone configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the first reaction zone where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and/or NO_X into the first reaction zone, the gas being at temperature(s) typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. rendering the gas free of reacted and unreacted sorbent;

E. venting the gas from the first reaction zone;

F. introducing sorbent and the gas from the first reaction zone into the second reaction zone, the gas being at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrates of manganese to substantially strip the gas of NO_X thereby loading the sorbent;

H. rendering the gas free of reacted and unreacted sorbent nitrates of manganese; and

I. venting the gas from the second reaction zone.

53. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, the system being comprised of;

i. at least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

ii. a modular reaction unit comprised of at least 3 interconnected bag houses, the bag houses being connected so that a gas containing SO_X and/or NO_X can be routed through any one of the bag houses, any two of the bag houses in series, or all of the at least three bag houses in series or in parallel, or any combination of series and parallel, each bag house being separately connected to the feeder so that sorbent can be introduced into each bag house where SO_X and/or NO_X capture can occur when the gas is contacted with sorbent for a time sufficient to allow formation of sulfates of manganese, nitrates of manganese, or both; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent in a gas containing SO_X and/or NO_X into a first bag house of at least three interconnected bag houses, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. rendering the gas free of sorbent reacted with sulfates of manganese;

E. venting the gas from the first bag house;

F. introducing sorbent and the gas from the first bag house into a second bag house, the gas being at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of sorbent reacted with nitrates of manganese; and

I. venting the gas from the second bag house.

54. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, the system being comprised of;

i. at least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g; and

ii. a modular reaction unit comprised of at least three (3) interconnected bag houses, the bag houses being connected so that a gas containing SO_X and/or NO_X can be routed through any one of the bag houses, any two of the bag houses in series, or all of the at least three bag houses in series or in parallel, or any combination of series and parallel, each bag house being separately connected to the feeder so that sorbent can be introduced into each bag house where SO_X and/or NO_X capture can occur when the gas is contacted with sorbent for a time sufficient to allow formation of sulfates of manganese, nitrates of manganese, or both, with SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, the bag houses each being configured to render the gas that has been substantially stripped of SO_X and/or NO_X free of reacted and unreacted sorbent so that the gas that has been substantially stripped of SO_X and/or NO_X may be vented from the bag houses or passed from one bag house to another bag house in series; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent in a gas containing SO_X and/or NO_X into a first bag house of at least three interconnected bag houses, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. rendering the gas free of sorbent reacted with sulfates of manganese;

E. venting the gas from the first bag house;

F. introducing sorbent and the gas from the first bag house into a second bag house, the gas being at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of sorbent reacted with nitrates of manganese; and

I. venting the gas from the second bag house.

55. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases, the system being comprised of;

i. at least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a first bag house configured for introduction of sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X;

the first bag house being configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted sorbent so that the gas can be directed out of the first bag house free of reacted and unreacted sorbent;

iii. a second bag house and a third bag house each connected to the first bag house by a common conduit, where the gas that has been substantially stripped of SO_X in the first bag house is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second and third bag houses each being configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second and third bag houses free of reacted and unreacted sorbent; and

iv. a diverter valve positioned in the common conduit so as to direct the flow of gas from the first bag house to the second bag house and/or the third bag house, the diverter valve having variable positions, in one position gas from the first bag house is directed to the second bag house, in another position gas from the first bag house is directed to both the second and third bag houses, and in a further position gas from the first bag house is directed to the third bag house;

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and/or NO_X into the first bag house, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. rendering the gas free of sorbent reacted with sulfates of manganese;

E. venting the gas from the first bag house;

F. directing the gas to the second bag house and/or the third bag house;

G. introducing sorbent and the gas from the first bag house into the second bag house and/or the third bag house, the gas being at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

H. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

I. rendering the gas free of sorbent reacted with nitrates of manganese; and

J. venting the gas from the second bag house and/or the third bag house.

56. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for removal of oxides of sulfur (SO_X) and oxides of nitrogen (NO_X) from gases, the system being comprised of;

i. at least one feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a first bag house configured for introduction of sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X;

the first bag house being configured to render the gas that has been substantially stripped of SO_X free of reacted and unreacted sorbent so that the gas can be directed out of the first bag house free of reacted and unreacted sorbent;

iii. a second bag house and a third bag house each connected to the first bag house by a common conduit, where the gas that has been substantially stripped of SO_X in the first bag house is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second and third bag houses each being configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second and third bag houses free of reacted and unreacted sorbent;

iv. a diverter valve positioned in the common conduit so as to direct the flow of gas from the first bag house to the second bag house and/or the third bag house, the diverter valve having variable positions, in one position gas from the first bag house is directed to the second bag house, in another position gas from the first bag house is directed to both the second and third bag houses, and in a further position gas from the first bag house is directed to the third bag house; and

V. at least one off-line loading circuit for pre-loading of sorbent on to fabric filter bags mounted within the second and third bag houses when the bag houses are off-line, the off-line loading circuit being comprised of;

a. an off-line loading circuit conduit configured for introduction of sorbent, the loading circuit conduit having a first end and a second end, the first end being connected to the feeder and the second end being connected to the bag houses;

b. a recirculation fan for blowing air and sorbent into each of the second and third bag houses to pre-load sorbent onto the filter fabric bags mounted therein;

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and/or NO_X into the first bag house, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. rendering the gas free of sorbent reacted with sulfates of manganese;

E. venting the gas from the first bag house;

F. directing the gas to the second bag house and/or the third bag house;

G. introducing sorbent and the gas from the first bag house into the second bag house and/or the third bag house, the gas being at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

H. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

I. rendering the gas free of sorbent reacted with nitrates of manganese; and

J. venting the gas from the second bag house and/or the third bag house.

57. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a first bag house configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

iii. a second bag house zone configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the first reaction zone where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second reaction zone being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and/or NO_X into the first bag house, the gas being at temperature(s) typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X thereby loading the sorbent;

D. rendering the gas free of reacted and unreacted sorbent;

E. venting the gas from the first bag house zone;

F. introducing sorbent and the gas from the first bag house into the second bag house, the gas being at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrate of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of reacted and unreacted sorbent; and

I. venting the gas from the second bag house zone.

58. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a cyclone/multiclone configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

iii. a bag house configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the cyclone/multiclone where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and/or NO_X into the cyclone/multiclone, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. rendering the gas free of reacted and unreacted sorbent;

E. venting the gas from the cyclone/multiclone;

F. introducing sorbent and the gas from the cyclone/multiclone into the bag house, the gas being introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrate of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of reacted and unreacted sorbent reacted with nitrates of manganese;

I. venting the gas from the bag house zone.

59. A process for dry removal of SO_X and NO_X from a gas stream, comprising the steps of:

A. providing an adaptable system for dry removal of oxides of sulfur (SO_X) and/or oxides of nitrogen (NO_X) from gases with minimal differential pressure across the system, comprising;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a section of serpentine pipe configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X; and

iii. a bag house configured for introduction of sorbent and the gas that has been substantially stripped of SO_X from the section of serpentine pipe, where the gas is introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of sorbent so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X and/or NO_X into the section of serpentine pipe, the gas being at temperature(s) typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X;

D. introducing the sorbent and the gas from the section of serpentine pipe into the bag house, the gas being introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

E. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrate of manganese to substantially strip the gas of NO_X;

F. rendering the gas free of reacted and unreacted sorbent;

G. venting the gas from the bag house.

60. A process for dry removal of SO_X, NO_X, mercury compounds, and ash from a gas stream, comprising the steps of:

A. providing an adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury in elemental, particulate and compound forms, and ash from gases with minimal differential pressure across the system, comprising;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. at least one bag house configured for introduction of the sorbent and the gas containing SO_X, NO_X, mercury, mercury compounds and ash where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decompostion temperature(s) of nitrates of manganese and contacted with the sorbent for a time to sufficient to simultaneously effect elemental mercury oxidation, SO_X capture at a targeted SO_X capture rate set point, and NO_X capture at a targeted NO_X, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury, the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and a gas containing SO_X, NO_X, mercury compounds, and ash, the gas being at temperatures typically ranging from ambient temperature to below the thermal decomposition of NO_X;

C. contacting the gas with sorbent for a time sufficient to simultaneously effect the capture of SO_X, NO_X and mercury compounds, the SO_X capture at a targeted SO_X capture rate set point, NO_X capture at a targeted NO_X capture rate set point and the capture of mercury compounds, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip mercury compounds from the gas;

D. rendering the gas free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash;

E. venting the gas from the bag house.

74. The process of any one of claims 60 to 65, wherein the process further comprises the steps of:

removing NO_X, SO_X and mercury reacted sorbent from a reaction zone of the system;

heating the sorbent to a first temperature to desorb NO₂ which is routed for further processing into marketable products;

heating the sorbent to a second temperature to desorb elemental mercury which is routed to a condenser for recovery;

rinsing the sorbent to wash away any ash and to dissolve sulfates of manganese into solution to form a liquor;

separating any ash in the liquor, the separated ash being routed for further handling;

adding alkali or ammonium hydroxide to the liquor to form an unreacted sorbent precipitate of oxides of manganese and a liquor containing alkali or ammonium sulfates, the liquor containing rinsed sorbent;

separating the rinsed sorbent and unreacted sorbent precipitate from the liquor, the liquor being routed for further processing into marketable products or for distribution and/or sale as a useful by-product;

drying the rinsed sorbent and sorbent precipitate to form unreacted sorbent; and

pulverizing the unreacted sorbent to de-agglomerate the unreacted sorbent.

75. The process of any one of claims 60 to 65, wherein the process further comprises the steps of:

removing NO_X, SO_X and mercury reacted sorbent from a reaction zone of the system;

heating the sorbent to a first temperature to desorb NO₂ which is routed for further processing into marketable products;

heating the sorbent to a second temperature to desorb mercury vapor; and

routing the mercury vapor condensing the mercury to recover marketable liquid mercury.

61. A process for dry removal of SO_X, NO_X, mercury compounds, and ash from a gas stream, comprising the steps of:

A. providing an adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury in elemental, particulate and compound forms, and ash from gases with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m2/g;

ii. a first bag house configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect elemental mercury oxidation, and SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury oxide(s) and salts of mercury, the first bag house being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash so that the gas may be vented from the first bag house; and

iii. a second bag house configured for introduction of sorbent and the gas vented from the first bag house where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and the gas containing SO_X and/or NO_X into the first bag house, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X and to effect capture of mercury compounds, the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury compounds from the gas;

D. rendering the gas free of reacted and unreacted sorbent, mercury oxide(s), ash, and sulfates of manganese;

E. venting the gas from the first bag house;

F. introducing sorbent and the gas from the first bag house into the second bag house, the gas being introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrate of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of reacted and unreacted sorbent;

I. venting the gas from the second bag house.

62. A process for dry removal of SO_X, NO_X, mercury compounds, and ash from a gas, comprising the steps of:

A. providing an adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury in elemental, particulate and compound forms, and ash from gases with minimal differential pressure across the system;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a cyclone/multiclone configured for introduction of the sorbent and a gas containing SO_X, NO_X, mercury compounds, and ash, where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury oxide(s) and salts of mercury, the cyclone/multiclone being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash so that the gas may be vented from the cyclone/multiclone; and

iii. a bag house configured for introduction of sorbent and the gas vented from the cyclone/multiclone where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and the gas into the cyclone/multiclone, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X and to effect capture of mercury compounds, the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury compounds;

D. rendering the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury oxide(s), ash, and salts of mercury;

E. venting the gas from the cyclone/multiclone;

F. introducing sorbent and the gas from the cyclone/multiclone into the bag house, the gas being introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrate of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of reacted and unreacted sorbent;

I. venting the gas from the bag house zone wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

63. A process for dry removal of SO_X, NO_X, mercury compounds, and ash from a gas stream, comprising the steps of:

A. providing an adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury in particulate, compound and elemental forms, and ash from a gas with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. at least one bag house configured for introduction of the sorbent and the gas containing SO_X, NO_X, mercury in elemental, particulate, and compound forms, and ash where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of nitrates of manganese and contacted with the sorbent for a time to sufficient to simultaneously effect SO_X capture at a targeted SO_X capture rate set point and NO_X capture at a targeted NO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury, the bag house being further configured to render the gas that has been substantially stripped of SO_X and NO_X free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury and ash so that the gas may be vented from the bag house; and

iii. a mercury-alumina reactor configured for introduction of the gas vented from the bag house and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury compounds in the gas, the mercury compounds being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been substantially stripped of mercury free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

B. introducing sorbent and the gas containing SO_X, NO_X, mercury compounds, and ash into the bag house, the gas being introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperatures(s) of nitrates of manganese;

C. contacting the gas with sorbent for a time sufficient to simultaneously effect the capture of SO_X, NO_X and mercury compounds, the SO_X capture at a targeted SO_X capture rate set point, NO_X capture at a targeted NO_X capture rate set point and the capture of mercury compounds, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the mercury compounds being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip mercury from the gas;

D. rendering the gas free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash;

E. venting the gas from the bag house;

F. introducing the gas vented from the bag house and alumina into the mercury-alumina reactor, the gas being introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface of alumina occurs;

G. contacting the gas with the alumina for a time sufficient to effect the capture of mercury in the gas, the mercury being captured by adsorption to the surface of alumina to substantially strip the gas of mercury, thereby loading the alumina;

H. rendering the gas free of reacted and unreacted alumina;

I. venting the gas from the reactor.

76. The process of any one of claims 63-64, wherein the process further comprising the steps of:

removing the alumina from the reactor;

heating the alumina to desorb mercury vapor;

condensing the mercury vapor to recover marketable liquid mercury.

Returning the regenerated alumina to the Hg-alumina reactor

64. A process for dry removal of SO_X, NO_X, mercury, and ash from a gas stream, comprising the steps of:

A. providing an adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in elemental, particulate, and compound form, mercury vapor, and ash from gases with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a first bag house configured for introduction of the sorbent and a gas containing SO_X and NO_X where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury oxide(s) and salts of mercury, the first bag house being further configured to render the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash so that the gas may be vented from the first bag house;

iii. a second bag house configured for introduction of sorbent and the gas vented from the first bag house where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the second bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the second bag house; and

iv. a mercury-alumina reactor configured for introduction of the gas vented from the second bag house and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury in the gas, the mercury being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been substantially stripped of mercury free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and the gas into the first bag house, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X and to effect the capture of mercury, the mercury being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury;

D. rendering the gas that has been substantially stripped of SO_X and mercury compounds free of reacted and unreacted sorbent, mercury oxide(s), ash, and salts of mercury;

E. venting the gas from the first bag house;

F. introducing the sorbent and the gas from the first bag house into the second bag house zone, the gas being introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrate of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of reacted and unreacted sorbent;

I. venting the gas from the second bag house;

J. introducing the gas vented from the second bag house and alumina into the mercury-alumina reactor, the gas being introduced below the temperature at which desorption of mercury adsorbed on the surface of alumina occurs;

K. contacting the gas with the alumina for a time sufficient to effect the capture of mercury in the gas, the mercury compounds being captured by adsorption to the surface of alumina to substantially strip the gas of mercury, thereby loading the alumina;

L. rendering the gas free of reacted and unreacted alumina;

M. venting the gas from the reactor.

65. A process for dry removal of SO_X, NO_X, mercury, and ash from a gas stream, comprising the steps of:

A. providing an adaptable system for the removal of oxides of sulfur (SO_X), oxides of nitrogen (NO_X), mercury compounds in elemental, particulate, and compound forms, and ash from a gas with minimal differential pressure across the system, the system being comprised of;

i. a feeder containing a supply of sorbent of regenerable oxides of manganese and/or regenerated oxides of manganese;

wherein the feeder is configured to handle and feed oxides of manganese which, upon regeneration, are in particle form and are defined by the chemical formula MnO_X, where X is about 1.5 to 2.0 and wherein the oxides of manganese have a particle size ranging from about 0.1 to about 500 microns and a BET value ranging from about 1 to about 1000 m²/g;

ii. a cyclone/multiclone configured for introduction of the sorbent and a gas containing SO_X, NO_X, mercury compounds, mercury vapor and ash, where the gas is introduced at temperatures typically ranging from ambient temperature to below the thermal decomposition temperature(s) of sulfates of manganese and contacted with the sorbent for a time sufficient to primarily effect SO_X capture at a targeted SO_X capture rate set point, the SO_X being captured by reacting with the sorbent to form sulfates of manganese to substantially strip the gas of SO_X and the mercury being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury oxide(s) and salts of mercury, the cyclone/multiclone being further configured to render the gas that has been substantially stripped of SO_X and mercury free of reacted and unreacted sorbent, mercury oxide(s), salts of mercury, and ash so that the gas may be vented from the cyclone/multiclone;

iii. a bag house configured for introduction of sorbent and the gas vented from the cyclone/multiclone where the gas is introduced at temperature(s) typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese and is further contacted with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point, the NO_X being captured by reacting with the sorbent to form nitrates of manganese to substantially strip the gas of NO_X, and the bag house being further configured to render the gas that has been substantially stripped of NO_X free of reacted and unreacted sorbent so that the gas may be vented from the bag house; and

iv. a mercury-alumina reactor configured for introduction of the gas vented from the second bag house and alumina, where the gas is introduced at temperature(s) typically below the temperature at which desorption of mercury adsorbed on the surface of alumina occurs and is contacted with alumina for a time sufficient to effect the capture of mercury in the gas, the mercury being captured by adsorption on the surface of alumina, the reactor being further configured to render the gas that has been partially substantially stripped of mercury free of reacted and unreacted alumina so that the gas may be vented from the reactor, wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level;

B. introducing sorbent and the gas into the cyclone/multiclone, the gas being at temperatures typically ranging from ambient to a temperature below the thermal decomposition temperature(s) of sulfates of manganese;

C. contacting the gas with sorbent for a time sufficient to effect SO_X capture at a targeted SO_X capture rate set point through the formation of sulfates of manganese to substantially strip the gas of SO_X and to effect capture of mercury, the mercury being captured in particulate form and by reacting with the sorbent to form mercury oxide(s) and salts of mercury to substantially strip the gas of mercury oxide(s) and salts of mercury;

D. rendering the gas free of reacted and unreacted sorbent, mercury oxide(s), ash, and salts of mercury;

E. venting the gas from the cyclone/multiclone;

F. introducing sorbent and the gas from the cyclone/multiclone into the bag house, the gas being introduced at temperatures typically ranging from ambient to below the thermal decomposition temperature(s) of nitrates of manganese;

G. contacting the gas with sorbent for a time sufficient to primarily effect NO_X capture at a targeted NO_X capture rate set point through the formation of nitrates of manganese to substantially strip the gas of NO_X;

H. rendering the gas free of reacted and unreacted sorbent;

I. venting the gas from the bag house;

J. introducing the gas vented from the bag house and alumina into the mercury-alumina reactor, where the gas is introduced below the temperature at which desorption of mercury adsorbed on the surface of alumina occurs;

K. contacting the gas with the alumina for a time sufficient to effect the capture of mercury in the gas, the mercury being captured by adsorption onto the surface of alumina to substantially strip the gas of mercury, thereby loading the alumina;

L. rendering the gas free of reacted and unreacted alumina;

M. venting the gas from the reactor.

89. An adaptable system for dry removal of pollutants from gases with minimal differential pressure across the system, comprising:

a. a feeder containing a supply of sorbent, the feeder being configured to handle and feed sorbent; and

b. a reaction zone configured for introduction of sorbent and a gas containing target pollutant, where gas is introduced and contacted with the sorbent for a time sufficient to effect capture of the target pollutant at a targeted pollutant capture rate; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

93. The system of any one of claims 89-92, wherein the system further comprises:

a mercury-alumina reactor

94. The system of any one of claims 89-92, wherein the system further comprises:

a control subelement for monitoring and adjusting process parameters

95. The system of any one of claims 89-92, wherein the system further comprises a control subelement for monitoring and regulating differential pressure.

96. A process for dry removal of target pollutants from a gas, comprising the steps of:

providing as system according to anyone of claims 89-92;

contacting a gas containing target pollutants with a sorbent to capture the target pollutant(s);

removing reacted sorbent from the system;

regenerating the sorbent; and

producing useful products.

90. An adaptable system for dry removal of pollutants from gases with minimal differential pressure across the system, comprising:

a. a feeder containing a supply of sorbent, the feeder being configured to handle and feed sorbent;

b. a first reaction zone configured for introduction of sorbent and a gas containing at least first and second target pollutants, where gas is introduced and contacted with the sorbent for a time sufficient to primarily effect capture of a first target pollutant at a target pollutant capture rate; and

c. a second reaction zone configured for introduction of sorbent and a gas containing target pollutants, where gas is introduced and contacted with the sorbent for a time sufficient to primarily effect capture of a second target pollutant at a targeted pollutant capture rate; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.

91. An adaptable system for dry removal of pollutants from gases with minimal differential pressure across the system, comprising:

a. at least one feeder containing a supply of sorbent, the feeder being configured to handle and feed sorbent; and

b. a modular reaction unit comprised of at least three (3) interconnected reaction zones, the reaction zones being connected so that gas containing pollutants can be routed through any one of the reaction units, any two of the reaction units, or all of the reaction units in series, in or in any combination of series and parallel, each reaction zone being separately connected to the feeder so that sorbent can be introduced into the reaction zone where capture of pollutants can tQ occur when the gas is contacted with the sorbent; and

wherein differential pressure within the system is regulated so that differential pressure across the system is no greater that a predetermined level.

92. An adaptable system for dry removal of pollutants from gases with minimal differential pressure across the system, comprising:

a. at least one feeder containing a supply of sorbent, the feeder being configured to handle and feed sorbent;

b. a first reaction zone configured for introduction of sorbent and a gas containing at least first and second target pollutants, where gas is introduced and contacted with the sorbent for a time sufficient to effect capture of at least the first target pollutant;

c. a second and a third reaction zone each connected to the first reaction zone by a common conduit and configured for introduction of sorbent and gas passing from the first reaction zone, where the gas passing from the first reaction zone is introduced and contacted with the sorbent for a time sufficient to effect capture of a least the second target pollutant;

d. a diverter valve for directing the flow of gas from the first reaction zone; and

wherein differential pressure within the system is regulated so that any differential pressure across the system is no greater than a predetermined level.