Abstract:
A method for removing mercury from flue gases generated by the combustion of coal comprises: storing a starter batch of activated carbon in an agglomerated state; de-agglomerating the starter batch in a separation device to create a contact batch of activated carbon; transporting the contact batch to a contact location; injecting the contact batch into contact with the flue gas at a contact location having a temperature between 400° F. and 1100° F., whereupon the activated carbon of the contact batch adsorbs mercury from the flue gas; and removing the activated carbon having mercury adsorbed thereon from the flue gas. The transporting step is conducted with substantially no intermediate storage of the contact batch following the de-agglomeration of the starter batch to prevent re-agglomeration of the activated carbon prior to injection.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    This application is a continuation of U.S. patent application Ser. No. 10/961,697, filed Oct. 8, 2004, which is a continuation-in-part of U.S. patent application Ser. No. 10/453,140, filed Jun. 3, 2003, both of which are incorporated by reference herein in their entirety. 
     
    
     BACKGROUND OF THE INVENTION 
       [0002]    The present invention relates to apparatus and a method for removing mercury from the products of solid fuel combustion including flue gases and more particularly to apparatus and a method for removing elemental mercury or mercury compounds from the flue gases from coal combustion. 
         [0003]    The use of activated carbon for the adsorption of mercury vapor has been successfully demonstrated in various applications such as municipal waste incineration. However, there are significant differences in the concentration of mercury from waste incinerators compared to coal-fired power plants with the concentration from the coal-fired power plants being anywhere from 10 to 100 times lower. Also, the mercury from waste incinerators is usually in the form of mercury chloride whereas the mercury from coal-fired power plants is usually in the form of elemental mercury. Both of these differences make it more difficult to remove the mercury from the flue gas from a coal-fired power plant. 
         [0004]    The utilization factor for activated carbon is limited by the relatively large particle size and low surface area which limits the adsorption of mercury. Using activated carbon with mean particle size of about 5 microns with a top size of about 10 microns would improve the mercury capture efficiency, but storage, handling, transport and dispersion of these articles is extremely difficult. As a result, the use of activated carbon for mercury capture in coal-fired power plants is too costly. In such applications, the utilization of the activated carbon is quite low with a minimum mole ratio of carbon to mercury of 10,000 to 1. 
         [0005]    Another form of carbon which has been proposed for the capture of mercury from flue gases is carbon black. Carbon black is a finely divided form of carbon produced by the incomplete combustion or thermal decomposition of a hydrocarbon fuel. The most common form of carbon black is referred to as furnace black or soot which is made by burning natural gas or petroleum oil in a closed furnace with about 50% of the air required for complete combustion. The external surface area of the carbon black is about 100 times that of activated carbon. This could result in a significant decrease of the C/Hg mole ratio for effective mercury capture compared to activated carbon. As the market price for carbon black is similar to that for activated carbon, there is the potential for a significant cost reduction. 
         [0006]    Carbon black generation for the capture of mercury from a refuse incinerator is disclosed in the International Patent Application PCT/SE93/00163 (International Publication Number WO 93/20926). This is characterized by the burning of a fuel with a deficiency of oxygen in a separate incinerator and injecting the soot-laden flue gas into the flue gas from the refuse incinerator. However, oxygen deficient combustion leads to the generation of other pollutants such as carbon monoxide and unburned hydrocarbons. Even if the flue gas from the carbon black generator were to be injected upstream of an acid gas removal device such as a flue gas scrubber, the carbon monoxide and unburned hydrocarbons would not be destroyed or removed. 
         [0007]    Another problem with the application of prior art carbon black and activated carbon-based methods for mercury capture from incinerators to the capture of mercury from coal-fired power plants is that refuse incinerators have high chlorine levels and the mercury is present in the flue gas predominantly as mercury chloride as previously stated. In coal-fired power plants, the mercury is usually elemental. Although carbon black and activated carbon have a relatively high affinity for the adsorption of mercuric chloride, they have a relatively lower affinity for the adsorption of elemental mercury. 
         [0008]    Carbon-based sorbents such as activated carbon have been proposed for controlling vapor phase mercury emissions in power plant flue gases. In a conventional method, carbon sorbents are injected in the flue gas duct upstream of particulate removal device such as baghouses and electrostatic precipitators and downstream of air heaters. 
         [0009]    The temperature of the location at which carbon sorbents are injected has heretofore been taken into consideration for the reason that it has been suggested that the adsorption capacity of mercury on carbon sorbents is higher at relatively lower temperatures. In this connection, it is also known in the art that physical adsorption (physisorption) of mercury on carbon is reduced with temperature. Consequently, the prior art essentially does not provide any detailed information concerning the desirability of injecting, for the purpose of capturing mercury from gas streams, carbonaceous sorbents at relatively higher temperatures such as, for example, temperatures above about 400° F. 
         [0010]    It is also known in the art that vapor phase mercury in the flue gas emerging from the high temperature boiler is in the form of elemental mercury. Oxidation of elemental mercury to oxidized mercury (Hg 2+ ) is beneficial to mercury control since it can be removed more easily by carbonaceous material. 
         [0011]    The injection of activated carbon into the flue gas may typically lead to a presence of, or an increase in, carbon in the fly ash, whereupon an amount of carbon in the fly ash above a prescribed limit may prevent the use of this fly ash for the purpose, for example, of concrete manufacturing. The activated carbon, because of its hydrophobic nature, adsorbs air-entraining additives that are used in the concrete formulation. Also due to activated carbon, the fly ash changes its color to dark grey to black. One way of minimizing this air entrainment impact is to oxidize the carbon, making it more hydrophilic. Another way to make the carbon hydrophilic is by impregnating the carbonaceous sorbent with additives that are hydrophilic, e.g., halide salts such as iron chloride. Still another way of minimizing this problem is to reduce the usage of carbon sorbent below a level that impacts air entrainment behavior and discoloration. 
       SUMMARY OF THE INVENTION 
       [0012]    An object of the present invention is to provide a method for the capture of mercury from a coal-fired power plant with carbonaceous sorbent without emitting pollutants generated in the production of the carbonaceous sorbent. The invention also may involve the treatment of the carbonaceous sorbent to enhance the capture of elemental mercury. 
         [0013]    In one aspect of the present invention, a method for removing mercury from flue gases generated by the combustion of coal comprises: storing a starter batch of activated carbon in an agglomerated state; de-agglomerating the starter batch in a separation device to create a contact batch of activated carbon; injecting the contact batch into contact with the flue gas at a contact location having a temperature between 400° F. and 1100° F., whereupon the activated carbon of the contact batch adsorbs mercury from the flue gas; transporting the contact batch to the contact location with substantially no intermediate storage of the contact batch following the de-agglomeration of the starter batch to prevent re-agglomeration of the activated carbon prior to injection; and removing the activated carbon having mercury adsorbed thereon from the flue gas. 
         [0014]    In another aspect, a method for removing mercury from flue gases generated by the combustion of coal comprises: milling a starter batch of activated carbon to provide a contact batch of activated carbon having a median particle size (d50) less than 15 microns, where d50 represents 50% of the particles by mass in the contact batch, the starter batch having a greater median particle size than the contact batch; injecting the contact batch into contact with the flue gas at a contact location having a temperature between 400° F. and 1100° F., whereupon the activated carbon of the contact batch adsorbs mercury from the flue gas; transporting the contact batch to the contact location with substantially no intermediate storage of the contact batch following the reduction of the starter batch to prevent agglomeration of the activated carbon prior to injection; and removing the activated carbon having mercury adsorbed thereon from the flue gas at a removal location having a removal temperature between 120 to 400° F. 
         [0015]    The present invention exploits the recognition that carbon sorbents may also be used to effect chemisorption of mercury onto their surfaces. Contrary to physisorption, the extent of chemisorption tends to increase with temperature and the present invention thus provides a process for exploiting the adsorption (both chemisorption and physisorption) of mercury takes place at a wider temperature range of 100° F. to 800° F. 
         [0016]    Equilibrium calculations of potential mercury species present in coal combustion flue gases show lower temperatures favor more complete conversion to oxidized mercury. However, the present invention has led to the recognition that kinetics of oxidation is not favored as the flue gas is cooled, even though equilibrium would indicate complete oxidation as well as the recognition that oxidized mercury species (HgCl 2 ) already begin to form at temperatures lower than about 600° C. (873 K) from elemental mercury. In accordance with this recognition that higher temperatures will favor kinetics of this transformation, the process of the present invention utilizes the entire temperature range of 300 to 1,000° F. to oxidize and capture mercury. 
         [0017]    An object of the present invention is to reduce consumption of carbon sorbent for both fabric filters and, in particular, electrostatic precipitators for a prescribed degree of vapor phase mercury removal. 
         [0018]    Another object of the present invention is to increase the oxidation degree of vapor phase mercury and decrease the amount of vapor phase elemental mercury. 
         [0019]    A further object of the present invention is to minimize the impact of carbon sorbent injection on the utilization of fly ash. 
         [0020]    Other objects and advantages of the invention will become apparent from the drawings and specification. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0021]    The present invention may be better understood and its numerous objects and advantages will become apparent to those skilled in the art by reference to the accompanying drawings in which: 
           [0022]      FIG. 1  is a schematic diagram of a first embodiment of a system in accordance with the present invention for removing elemental mercury or mercury compounds from the flue gases from coal combustion; 
           [0023]      FIG. 2  is a schematic diagram of a second embodiment in accordance with the present invention of a system for removing elemental mercury or mercury compounds from the flue gases from coal combustion; 
           [0024]      FIG. 3  is a schematic diagram of a third embodiment of a system in accordance with the present invention for removing elemental mercury or mercury compounds from the flue gases from coal combustion; 
           [0025]      FIG. 4  is a schematic diagram of the ash disposal system of  FIGS. 1-3 ; 
           [0026]      FIG. 5  is a schematic diagram of an optional SO 3  (sulfur trioxide) sorbent addition subsystem; 
           [0027]      FIG. 6  is a graph illustrating the effect of sorbent particle size and halogen treatment on mercury capture; 
           [0028]      FIG. 7  is a graph illustrating the effect of dispersion on in-situ particle size distribution; 
           [0029]      FIG. 8  is a schematic diagram of a fourth embodiment of a system in accordance with the present invention for removing elemental mercury or mercury compounds from the flue gases from coal combustion; 
           [0030]      FIG. 9  is a graph illustrating conversion (%) of soot, CO, and HC as a function of temperature (° C.); 
           [0031]      FIG. 10  is a graph illustrating a typical destruction profile for CO and HC with a PGM catalyst; 
           [0032]      FIG. 11  is a graph illustrating examples of the exposure temperature of sorbents in accordance with the present invention for air heater-ESP, air heater-spray dryer-ESP and hot ESP configurations; 
           [0033]      FIG. 12  is a graph illustrating a thermo-gravimetric analysis of the sorbent in the form of fine activated carbon in 5% O 2  in N 2  to determine its ignition temperature; 
           [0034]      FIG. 13  is a schematic illustration of an arrangement having a sorbent injection location corresponding to the selectively determined process limits; 
           [0035]      FIG. 14  is a schematic illustration of an arrangement including an SCR and having a sorbent injection location; 
           [0036]      FIG. 15  is a graph illustrating the results of a trial to determine mercury capture efficiency by a first group of injected carbon sorbent that are deemed to be the group of in-flight sorbent particles and a second group of injected carbon sorbent that are deemed to be the group of deposited sorbent particles; 
           [0037]      FIG. 16  is a schematic illustration of a plurality of multiple injection ports provided to uniformly distribute sorbent particles across the cross section of the flue gas flow; 
           [0038]      FIG. 17  is a schematic illustration of a slurry injection for enhanced sorbent deposition; 
           [0039]      FIG. 18  is a schematic illustration of a precharging of sorbent particles; 
           [0040]      FIG. 19  is a perspective view of a small portion of the injected sorbent as it coats the air heater elements and of the balance of the sorbent particles as they are entrained by preheated air; 
           [0041]      FIG. 20  is a schematic illustration of a combination of flue gas side injection with air-side injection helps control mercury for plant configurations with hot-side ESPs; 
           [0042]      FIG. 21  is a schematic top plan view of the sequential operation of a sorbent injection lance system for a rotary regenerative air heater; 
           [0043]      FIG. 22  is a schematic view of air-side injection of products from an on-site sorbent generation and treatment unit; and 
           [0044]      FIG. 23  is a schematic view of multiple sorbent injection for a rotary regenerative air heater. 
       
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
       [0045]    With reference to  FIG. 1 , there is illustrated therein an exemplary fuel conversion arrangement for converting a fuel—namely, a solid fossil fuel in the form of coal—into a desired energy form. The exemplary fuel conversion arrangement illustrated in  FIG. 1  effects the fuel conversion via combustion of coal and is illustratively configured as a typical 100 MWe coal firing plant  10  which combusts approximately 40 tons/hr of coal with a flue gas flow  12  of about 350,000 Nm 3 /hr. The raw coal is fed  14  to a pulverizer/crusher  16  where the raw coal is reduced to particulate size. Primary air carries the coal particulates from the pulverizer/crusher  16  to the boiler  18 , where the coal is burned to convert water into steam. The temperature of the flue gases leaving the boiler/furnace  18  ranges from 1400 to 2200° F. The flue gases are cooled in the superheater and convective pass  20  (economizer/re-heater) to around 600 to 800° F. before entering the air preheater  22 . Flue gas temperatures exiting the air preheater  22  and entering the electrostatic precipitator (ESP)/fabric filter  24  range from 220 to 370° F. If the sorbent requirement for mercury capture were 1 lb./MMacf, about 20 lb/hr of sorbent would need to be injected. At 5 lb/MMacf (120 mg/Nm 3 ), the sorbent requirement would be 100 lb/hr. 
         [0046]    In a first embodiment of a system  26  for removing elemental mercury or mercury compounds, a starter batch of carbonaceous sorbent is in the form of carbonaceous sorbent  28  stored in a silo  30 , with the carbonaceous sorbent  28  being in an agglomerated state because the very small particles thereof tend to stick to each other. Accordingly, the starter batch of the sorbent  28  is fed by a feeder  32  to a separation device  34 , which comminutes (if necessary) and de-agglomerates the sorbent particles  28  into a contact batch of carbonaceous sorbent and a retained batch of carbonaceous sorbent. The contact batch of carbonaceous sorbent has a particle size distribution of carbonaceous sorbent of d 50 &lt;15 microns, where d 50  represents 50% of the particles by mass in the entire distribution in the contact batch with the particle size distribution of carbonaceous sorbent in the contact batch after separation being less than the particle size distribution of carbonaceous sorbent in the starter batch before separation and less than the particle size distribution of carbonaceous sorbent in the retained batch. 
         [0047]    This device  34  may be a particle-particle separator or a jet mill, where compressed air or high-pressure steam is the energy source. The separation device  34  performs three functions: particle-particle separation; particle size reduction; and classification of fine particles to “product” and either return of the coarse particles to the silo  30  or retention of the coarse particles within the separation device  34  for further processing. 
         [0048]    The target particle size distribution is d 50 &lt;15 microns, preferably d 50 &lt;8 microns and most preferably d 50 &lt;4 micron, where d 50  represents 50% of the particles by mass in the entire distribution. Primary particle size reduction is required when the starting particle size distribution is larger than desired product size. No primary size reduction is required if the primary particle sizes are already smaller than the target product size, such as in the case of carbon black where the primary particle size less than 1 micron. The minimum energy input for this separation and optional size reduction device  34  is 10 kWh/ton, more preferably it is 100 kWh/ton, and most preferably it is 1000 kWh/ton. This energy input can be supplied via high pressure fluid such as steam or compressed air  36  in an air jet mill, or by media such as grinding balls or rollers in a ball mill or roller mill. 
         [0049]    In addition to handling thereof by the separation device  34 , the sorbent particles  28  are subjected to one or more processes before they are injected into the stream of flue gas. In one alternative, the sorbent particles  28  are sent along a path  38  from the silo  30  to an oxidizer unit  40 , where the particles are contacted by an oxidizing agent  42  (e.g., ozone, hydrogen peroxide, hot air, concentrated nitric acid), making the outer surfaces of the particles hydrophilic. The treated sorbent may then be fed along a path  44  to the separation device  34  or sent along a path  46  to a blender  48  where a solution  50  is sprayed  52  on the sorbent particles by a sprayer  54  to deposit a halogen on the surface of the sorbent particles  28 . The solution  50  is chosen from potassium iodide, iodine dissolved in potassium iodide, alkali halides (e.g., NaCl), and halide salts (e.g., CaCl 2 ), or halogen acids (e.g., HCl, Hl, HBr, HF) dissolved in water. A typical additive amount results in a halogen concentration in the sorbent of about 0 to 5 percent. The treated sorbent is then fed along a path  56  to the separation device  34 . 
         [0050]    A halogen  58 , such as chlorine, bromine, iodine or fluorine, may also be deposited on the sorbent  28  by vaporizing the halogen  58  in a vaporizer  60  and condensing/adsorbing it on the sorbent  28 . The vaporized halogen may be injected along a path  62  into the sorbent  28  between the particle oxidizer  40  (described above) and the feeder  32 , between the feeder  32  and the separation device  34 , or onto the “fines” and de-agglomerated particles leaving the separation device  34 . 
         [0051]    The effect of halogen treatment on mercury removal is shown in  FIG. 6  and Table 1.  FIG. 6  shows that treating coal sorbent  28  with iodine (0 to 2.5 weight percent) significantly improves sorbent performance. About 10 percent mercury removal was obtained with no iodine treatment for “fine” coal sorbent, while about 95 percent mercury removal was obtained with 2.0 percent iodine addition to “fine” coal sorbent. Table 1 shows the effect of halogen treatment for carbon black sorbent and activated carbon sorbent. For carbon black with a surface area of 100 m 2 /g and at a sorbent concentration of 50 mg/Nm 3  in the flue gas, addition of iodine to sorbent  28  (1 percent I 2  in carbon after treatment) improved the mercury removal performance from 20 percent to 100 percent. For activated carbon at a sorbent concentration of 100 mg/Nm 3  in the flue gas, addition of iodine to sorbent (1 percent I 2  in carbon after treatment) improved the mercury removal performance from 75 percent to 90 percent. 
         [0000]    
       
         
               
             
               
               
             
               
               
               
               
               
               
             
               
               
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Mercury Removal Efficiencies from an Air Stream with 
               
               
                 Various Sorbents and Sorbent Concentrations (~200° F.) 
               
             
          
           
               
                   
                 Sorbent Concentration 
               
               
                   
                 (mg/Nm 3 ) 
               
             
          
           
               
                 Sorbent 
                 0 
                 20 
                 35 
                 50 
                 100 
               
               
                   
               
             
          
           
               
                 Carbon Black (SA = 100 m 2 /g, d 50  &lt; 1 μm) 
                 0 
                 &lt;5 
                 — 
                 20 
                 30 
               
               
                 Carbon Black (SA = 500 m 2 /g, d 50  &lt; 1 μm) 
                 0 
                 &lt;5 
                 — 
                 20 
                 — 
               
               
                 Carbon Black (SA = 500 m 2 /g with 1% I 2   
                 0 
                 40 
                 60 
                 100 
                 100 
               
               
                 Carbon Black (SA = 100 m 2 /g with 1% I 2   
                 0 
                 20 
                 — 
                 100 
                 100 
               
               
                 Activated Carbon (d 50  = 18 μm) with 1% I 2   
                 0 
                 15 
                 — 
                 60 
                 90 
               
               
                 Activated Carbon (d 50  = 18 μm) 
                 0 
                 — 
                 — 
                 — 
                 75 
               
               
                   
               
               
                 *SA = Surface area; d 50  = Weight mean particle size 
               
             
          
         
       
     
         [0052]      FIG. 7  shows in-situ size distributions for two samples injected into a duct with different levels of energy used for particle-particle separation (de-agglomeration). The first sample is a “coarse” commercial powdered activated carbon, with a mean particle size (d 50 ) of 18 μm. The second sample is a “fine” sorbent with a mean particle size (d 50 ) of 3 μm. When either sample was injected into the duct with a low energy level being used for particle separation (“poor” dispersion), the actual size of particles observed in the duct was significantly coarser than when higher energy was used for particle separation (“high” dispersion). 
         [0053]    The static pressure of air leaving the separation device  34  is around 5 to 10 inches water gauge. This static head may be insufficient to transport and distribute the sorbent  28  via the injection lances into the flue gas duct. As seen in  FIG. 1 , a “dirty air” material-handling fan/blower  64  may be placed after the separation device  34  to increase the static head for sorbent transport and distribution. A static head of about 30 inches water gauge is preferred. 
         [0054]    The inventive apparatus also comprises a means for disposing the contact batch of carbonaceous sorbent into contact with the products of fuel conversion at a contact location such that the carbonaceous sorbent of the contact batch adsorbs mercury. Accordingly, the de-agglomerated sorbent  28  and the conveying air/steam is injected at a contact location  66  into the flue gas duct through such a means in the form of a distributor  68  having multiple lances. The injector tip is designed to impart a tangential momentum to the sorbent stream (swirl tip) and increase the rate of spread and distribution of the sorbent  28  in the flue gas stream  12 . The sorbent  28  may be injected into the flue gas stream  12  between the boiler  18  and the convective pass/superheater  20 , between the convective pass/superheater  20  and the air preheater  22 , or between the air preheater  22  and the ESP/fabric filter  24 . 
         [0055]    Thus, the system  26  for removing elemental mercury or mercury compounds handles carbonaceous sorbent  28  of a starter batch stored in a silo  30  in an agglomerated state. The sorbent  28  is fed by a feeder  32  to a separation device  34 , which comminutes (if necessary) and de-agglomerates the sorbent particles  28  to their primary size distribution. The de-agglomerated sorbent  28  of a contact batch created from the starter batch is then conveyed by the airsteam for injection at a contact location  66  in a flue gas duct whereat carbonaceous sorbent of the contact batch adsorbs mercury from the flue gas. Preferably, the transport means of the inventive apparatus which transports carbonaceous sorbent of the contact batch to the contact location operates to deliver, on average, at least ninety percent (90%) of the carbonaceous sorbent of the contact batch to the contact location  66  in less than thirty (30) minutes following the separation of the carbonaceous sorbent of the starter batch into the carbonaceous sorbent of the contact batch and the carbonaceous sorbent of the retained batch, more preferably operates to deliver, on average, at least ninety percent (90%) of the carbonaceous sorbent of the contact batch to the contact location  66  in less than five (5) minutes following the separation, and, most preferably, operates to deliver, on average, at least ninety percent (90%) of the carbonaceous sorbent of the contact batch to the contact location  66  in less than one (1) minute following the separation. 
         [0056]    In a second embodiment of a system for removing elemental mercury or mercury compounds in accordance with the present invention and shown in  FIG. 2 , hereinafter designated as a system  69  for removing elemental mercury or mercury compounds, a portion of the coal pulverized in the pulverizer  16  is extracted at a location  70  from the pulverizer exit as sorbent  28 . Preferably between 10 to 1000 lb/hr of coal (about 0.01 to 1.0 percent of total coal feed to boiler), more preferably between 50 and 500 lb/hr, and most preferably between 100 and 200 lb/hr is extracted at the location  70 . A blower  72  may be required to provide the necessary motive force for moving the extracted sorbent solids  28 . 
         [0057]    The extracted sorbent solids  28  are subjected to one or more processes. The sorbent solids  28  may be sprayed at a location  74  with a solution  50  to deposit a halogen on the surface of the sorbent particles  28 . The solution  50  is chosen from potassium iodide, iodine dissolved in potassium iodide, alkali halides (e.g. NaCl), and halide salts (e.g. CaCl 2 ), or halogen acids (e.g. HCl, Hl, HBr, HF) dissolved in water. A typical additive amount results in a halogen concentration in the sorbent  28  of about 0 to 5 percent. The treated sorbent  28  is then fed along a path  76  to the separation device  34 . 
         [0058]    A halogen  58 , such as chlorine, bromine, iodine or fluorine, may also be deposited on the sorbent by vaporizing the halogen in a vaporizer  60  and condensing/adsorbing it on the sorbent. The vaporized halogen may be injected at a location  78  into the sorbent  28  between the blower  72  and the separation device  34 , or onto the “fines” and de-agglomerated particles leaving the separation device  34 . 
         [0059]    A “dirty air” material-handling fan/blower  64  may be placed after the separation device  34  to increase the static head for sorbent transport and distribution. The de-agglomerated sorbent  28  and the conveying air/steam is injected into the flue gas duct through a distributor  68  similar to that of the first embodiment  26 . The sorbent  28  may be injected into the flue gas stream  12  between the boiler  18  and the convective pass/superheater  20 , between the convective pass/superheater  20  and the air preheater  22 , or between the air preheater  22  and the ESP/fabric filter  24 . 
         [0060]    In a third embodiment of a system for removing elemental mercury or mercury compounds in accordance with the present invention and shown in  FIG. 3 , hereinafter designated as a system  80  for removing elemental mercury or mercury compounds, a portion of the coal pulverized in the pulverizer  16  is also extracted at a location  82  from the pulverizer exit as sorbent  28 . Preferably between 10 to 1000 lb/hr of coal (about 0.01 to 1.0 percent of total coal feed to boiler), more preferably between 50 and 500 lb/hr, and most preferably between 100 and 200 lb/hr is extracted at the location  82 . A blower  84  may be required to provide the necessary motive force for moving the extracted sorbent solids  28 . 
         [0061]    The extracted coal is partially combusted in a char generator reactor  86  by subjecting the coal to temperatures between 300 and 1500° C. The air supply to the char generator  86  is limited to achieve only partial combustion of the coal, preferably only the volatile portion of the coal. Accordingly, air amounts are preferably controlled between 0.3 and 1.0 times the amount required for complete combustion of coal, and more preferably between 0.5 and 0.7 times the amount required for complete combustion of coal. 
         [0062]    The high temperatures of the solids and gases exiting along a path  88  the char generator  86  are reduced in a downstream cooling section  90 . Water quenching or an air-, water- or steam-cooled heat exchanger may be used to cool the gases and the solids. The temperature of the gases and solids exiting the cooling section  90  is preferably around 300° C. or lower. 
         [0063]    The cooled gases and solids (char) are then sent along a path  92  to a particle separator  94 , preferably a cyclone. The separated gases, with some fine particles, are discharged at a location  96  to the main boiler  18  to ensure complete combustion of the unburnt hydrocarbons and other combustible species like carbon monoxide and carbon. The particles  28  separated by the particle separator  94  are discharged along a path  98  to a silo  100 . Alternatively, the sorbent particles  28  may be discharged along a path  102  to an oxidizer unit  104 , where the particles  28  are contacted by an oxidizing agent  42  (e.g. ozone, hydrogen peroxide, hot air, concentrated nitric acid), making the outer surfaces of the particles hydrophilic. The treated sorbent is then discharged along a path  98  to the silo  100 . 
         [0064]    As the sorbent  28  is fed along a path  106  from the silo  100  to the flue gas stream  12 , a halogen is deposited on the outer surface of the sorbent particles  28 . In one alternative, the sorbent particles  28  are sent to a blender  48  where a solution  50  is sprayed on the sorbent particles  28  to deposit the halogen on the surface of the sorbent particles  28 . The solution  50  is chosen from potassium iodide, iodine dissolved in potassium iodide, alkali halides (e.g., NaCl), and halide salts (e.g., CaCl 2 ), or halogen acids (e.g., HCl, Hl, HBr, HF) dissolved in water. A typical additive amount results in a halogen concentration in the sorbent of about 0 to 5 percent. The treated sorbent  28  is then fed along a path  108  to the separation device  34  by a feeder  110 . 
         [0065]    Alternatively, the halogen (e.g., chlorine, bromine, iodine or fluorine) may be deposited on the sorbent by vaporizing the halogen  58  in a vaporizer  60  and condensing/adsorbing it on the sorbent  28 . The vaporized halogen may be injected at a location  112  into the sorbent  28  between the silo  100  and the feeder  110 , between the feeder  110  and the separation device  34  or onto the “fines” and de-agglomerated particles leaving the separation device  34 . 
         [0066]    A “dirty air” material-handling fan/blower  64  may be placed after the separation device  34  to increase the static head for sorbent transport and distribution. The de-agglomerated sorbent  28  and the conveying air/steam is injected into the flue gas duct through a distributor  68  similar to that of the first embodiment  26 . The sorbent  28  may be injected into the flue gas stream  12  between the boiler  18  and the convective pass/superheater  20 , between the convective pass/superheater  20  and the air preheater  22 , or between the air preheater  22  and the ESP/fabric filter  24 . 
         [0067]    In a fourth embodiment of a system for removing elemental mercury or mercury compounds in accordance with the present invention and shown in  FIG. 8 , hereinafter designated as a system  114  for removing elemental mercury or mercury compounds, the sorbent  28  has the most preferable particle size mercury removal system—namely, d 50 &lt;2 micron, where d 50  represents 50% of the particles by mass in the entire distribution—and this is achieved in this fourth embodiment by configuring the sorbent  28  as carbon black or soot. Compared to “coarse” and “agglomerated” activated carbon, much smaller quantities of carbon black/soot are required to capture a prescribed amount of mercury in boiler flue gases. For example, to remove 90% of elemental mercury, 50 mg/Nm 3  of impregnated carbon black are required compared to greater than 1000 mg/Nm 3  of “coarse” and “agglomerated” activated carbon. Also, much smaller quantities of oxidizing agents such as iodine would be required for impregnation of the sorbent  28  (less than 1% by weight of carbon) compared to activated carbon, where 1-10% by weight of carbon would be required. 
         [0068]    In a sub-assembly  116  of this system  114  for generating the sorbent  28  with a desirably very fine particle size distribution, a soot-generating device  118  is disposed within the high temperature region of the boiler  18 . An oxidizing region  120  of the boiler  18 , downstream of the soot device  118 , ensures that the CO and HC generated during the soot generating process are destroyed. With reference to  FIG. 9 , the temperature range in the oxidizing region is preferably 500 to 1000° C., and more preferably 600 to 800° C., to ensure minimal soot destruction and maximal CO/HC destruction. 
         [0069]    In an alternative sub-assembly  122  of this system  114  for generating the sorbent  28  with a desirably very fine particle size distribution, the carbon black/soot is generated in a separate soot generating device  124  having a CO/HC oxidation chamber  126 . The CO/HC oxidation chamber  126  may have an input  128  for receiving oxygen or air required to destroy the CO/HC. The residence time of the stream of carbon black/soot within the CO/HC oxidation chamber  126  and the temperature maintained in the CO/HC oxidation chamber  126  (preferably 500 to 1000° C., and more preferably 600 to 800° C.) are optimized to destroy the CO/HC with minimal soot destruction. 
         [0070]    In still another alternative sub-assembly  130  of this system  114  for generating the sorbent  28  with a desirably very fine particle size distribution, a catalytic reactor  132  for targeted CO and HC destruction is disposed between the soot generating device  134  and the flue gas stream  12 . One example of such a catalytic reactor  132  is a monolith (e.g. made of stainless steel or ceramic) coated with a variety of platinum group metals (e.g., platinum, rhodium, palladium). A typical destruction profile for CO and HC with a PGM catalyst is shown in  FIG. 10 . At the temperatures shown in  FIG. 10 , soot would not be destroyed to any significant extent. 
         [0071]    In conventional coal-fired plants, unburnt carbon arriving at the electrostatic precipitator (ESP) or fabric filter is predominantly in the form of the large coal particles that have not finished combustion. Fine particles of coal are rarely present in the normal application since they are completely burnt out. In conventional plants, therefore, the ash collected in the precipitator or fabric filter consists of predominantly larger carbon particles and smaller fly ash particles, which are very difficult to separate. 
         [0072]    In the mercury removal systems  26 ,  69 ,  80 ,  114  described above, the carbonaceous mercury sorbent  28  is generally manufactured external to the boiler/main combustor  18  and then subsequently reduced in size and then introduced into the flue gas stream  12 . The sorbent particles  28  are engineered to be extremely small and are therefore distinct from the ash and may be separated from the normal ash in the ash disposal system  136  shown in  FIGS. 1-3 . 
         [0073]    With reference to  FIG. 4 , the mercury-laden sorbent  28  is collected in the ESP/fabric filter  24 , along with fly ash  137 . The mercury-laden sorbent-fly ash mixture is transferred along a path  138  from the hopper  140  of the ESP/fabric filter  24  to an ash storage silo  142  and then fed along a path  144  with a feeder  146  to a classifier  148 , which is capable of separating the “fine” and low-density mercury sorbent  28  from the coarser and denser fly ash  137 . The classifier  148  is preferably of the dynamic type with a separately controlled classifier wheel, operating at tip speeds of preferably greater than 50 m/s and more preferably 100 m/s to ensure good separation and product recovery. 
         [0074]    A particle-particle separator  150  may be disposed between the silo  142  and the classifier  148 . The function of the particle-particle separator  150  is to separate the mercury-laden sorbent  28  from the fly ash  137 , which would have agglomerated as a result of being collected together in the ESP/fabric filter  24  and stored in the hopper  140  and silo  142 . A jet mill can be used for this purpose, although, little size reduction is required and therefore the energy consumption would be lower than if the particle size has to be reduced. 
         [0075]    As shown in  FIG. 1 , a SO3 (sulfur trioxide)-capturing sorbent  152  may be injected at a location  154  into the flue gas stream  12  along with or separate from the mercury sorbent  28 . With additional reference to  FIG. 5 , a system  156  for injecting the SO3 (sulfur trioxide)-capturing sorbent  152  includes a silo  158 . The SO3 (sulfur trioxide)-capturing sorbent  152  stored in the silo  158  is metered to the separation device  34  by a feeder  160 . The de-agglomerated particles  152  are then injected into the flue gas duct by the blower  64  and distributor  68 . A separation device, blower and distributor which are separate from the ones used by the mercury sorbent  28  may also be utilized (not shown). Alternatively a SO3 (sulfur trioxide)-capturing sorbent precursor  162  may be stored in the silo  158  and fed to a precursor converter  164 . For example, limestone  162  may be stored in the silo  158  and converted to lime  152  in a calciner  164 . It should be appreciated that the SO3 (sulfur trioxide)-capturing sorbent system  156  may be used with or separate from any of the mercury removal systems  26 ,  69 ,  80 ,  114 . 
         [0076]    In accordance with the present invention, treatment of the carbonaceous sorbent with additives may be undertaken to further improve the oxidation and capture of mercury. These additives include halogens (chlorine, bromine, iodine, fluorine) and halides (examples include ammonium chloride, ammonium bromide, iron chloride, iron bromide, zinc chloride), H2SO4 and H3PO4. These additives may be added (for example by spraying) to the carbonaceous material as a water-based solution or another solvent (such as alcohol)-based solution followed by evaporation of the water/solvent. An example for incorporating the additive into the carbonaceous material via a solution is iron chloride. 
         [0077]    Additives may also be added by mixing them with the carbonaceous sorbent and heating them to a temperature that will volatilize the additive locally but distribute it by subsequent adsorption on the carbon. It is preferred that the temperature to which the carbonaceous material and additive are heated is above 400° F. and most preferably above 500° F., to ensure that it will be stable when injected in the flue gas at those temperatures. An example of additive that can be incorporated in the above fashion is iodine or bromine. 
         [0078]    In accordance with the present invention, carbon-based sorbent is injected at a location where interaction between injected sorbent and mercury in flue gas is maximized both for (1) oxidation of mercury on sorbent surface and for (2) its subsequent capture by sorbent. The following three types of temperatures are preferably taken into account in determining the sorbent injection location: injection temperature, collection temperature and exposure temperature range. In this regard, the injection temperature is deemed to be the temperature of the location at which the sorbent and the flue gas are first in contact with one another. Also, the collection temperature is deemed to be the temperature of a given collection location at which carbonaceous sorbent having mercury absorbed thereon is separated from the flue gas either with or without other solids, gases, or liquids entrained with the flue gas. Accordingly, a given collection location may be a respective known particulate removal device such as a cyclone, an electrostatic precipitator (ESP), a baghouse, or a particulate scrubber. 
         [0079]    In connection with the capture of mercury in flue gas generated by the combustion of fossil fuels such as coal, it is believed that the sorbent injection temperature will typically be from 400 to 1100° F., and the sorbent collection temperature from 100 to 800° F. The exposure temperature range is bound by the injection temperature—namely, the flue gas temperature at which sorbent is injected—and the collection temperature—namely, the flue gas temperature at which the majority of the sorbent is removed from the flue gas. Additionally, the exposure temperature range (injection temperature minus collection temperature) should preferably be greater than 50° F., preferably greater than 100° F., and more preferably greater than 200° F. (temperature drop due to spray dryer excluded).  FIG. 11  shows examples of the exposure temperature of sorbents in accordance with the present invention for air heater-ESP, air heater-spray dryer-ESP and hot ESP configurations. 
         [0080]    Trials have shown that, with respect to the injection of activated carbon at temperatures higher than 400° F. into a flue gas obtained from the combustion of coal, mercury oxidation and removal were higher than if was injected at lower temperatures. 
         [0081]    There is an upper limit in temperature, however, to be taken into account in selecting the injection point. The selection of this limit takes into account the reaction of activated carbon with oxygen in the flue gas at high temperatures, which results in the consumption of the activated carbon. For example, subjecting activated carbon to increasing temperatures in a gas stream containing about 5 percent oxygen (typical for flue gas) may lead to weight loss above approximately 750° F. (see  FIG. 12 , which is a graph illustrating a thermo-gravimetric analysis of the sorbent in the form of fine activated carbon in 5% O2 in N2 to determine its ignition temperature). This provides a qualitative measure of the upper temperature limit. Since this exposure of the carbon in the boiler flue gas is more appropriately measured in seconds rather than minutes, it can be expected that the upper temperature limit will be higher closer to 1000° F. 
         [0082]    These temperature limits identify the preferred temperature range for carbon injection for mercury capture and oxidation. This range is preferably between 400° F. and 1100° F. and more preferably between 500° F. and 900° F. and most preferably between 550° F. and 750° F. While these temperature ranges are appropriate for the carbonaceous material used in the description of this example, it is to be understood that the above-identified temperature limits will differ for different types of carbonaceous material, for the gas compositions they are subjected, and the residence time the carbon is exposed at the high temperature. Hence, efficacious capture of mercury in flue gas via injection of a carbonaceous sorbent at relatively higher temperatures should be expected to be constrained only by the process limits such as noted above and not by the absolute specific temperature targets. 
         [0083]    An example of a sorbent injection location corresponding to the above-noted process limits is schematically shown in  FIG. 13 . In coal-fired boilers, coal is combusted to generate hot flue gas and the hot flue gas passes through a series of heat exchangers and its heat extracted to make superheated steam. The heat exchangers, in a typical conventional configuration, may consist, in a first portion thereof that is not illustrated herein, of a radiant furnace section (for saturated steam production), followed by convective superheater and reheater sections (for superheated steam production). A further downstream portion of the heat exchanger configuration, that is illustrated in  FIG. 13 , includes an economizer section  310  for preheating the water (before it goes to the radiant furnace for saturated steam production), and an air heater section  312  (for preheating the combustion air). For the limits identified, the optimum injection location of the carbonaceous sorbent into the flue gas stream is a location  314  between the economizer and the air heater. 
         [0084]    The carbonaceous sorbent injected in the flue gas is injected at the exit of the economizer  310 . It may be injected directly or treated for size reduction and de-agglomeration in a mill  316  as described below. In a variation of this embodiment of the process, the carbonaceous sorbent is injected in two or more locations, one of the locations being defined by the identified flue gas temperature limits. For example, as shown in  FIG. 13 , in addition to the injection location  314 , a second injection location  318  can be provided that is located downstream of the air heater  312  and upstream of a particulate collection device  320 . 
         [0085]    Another example of a sorbent injection location is schematically shown in  FIG. 14 , which illustrates a combustion and flue gas handling arrangement comprising a selective catalytic reactor (SCR). In this arrangement, the heat exchangers, in a typical conventional configuration, may consist, in a first portion thereof that is not illustrated herein, of a radiant furnace section (for saturated steam production), followed by convective superheater and reheater sections (for superheated steam production). A further downstream portion of the heat exchanger configuration, that is illustrated in  FIG. 14 , includes an economizer section  610  for preheating the water (before it goes to the radiant furnace for saturated steam production), and an air heater section  612  (for preheating the combustion air). For the limits identified, the optimum injection location of the carbonaceous sorbent into the flue gas stream is a location  614  between the economizer  610  and a selective catalytic reactor (SCR)  616 . 
         [0086]    The carbonaceous sorbent injected in the flue gas is injected at the exit of the economizer  610 . It may be injected directly or treated for size reduction and de-agglomeration in a mill  618 . 
         [0087]    The injection of carbon sorbent in flue gas in accordance with the present invention leads to two groups of carbon sorbent that can be characterized by their respectively different residence times in the boiler system: a first group of injected carbon sorbent that are deemed to be the group of in-flight sorbent particles and a second group of injected carbon sorbent that are deemed to be the group of deposited sorbent particles. The in-flight sorbent particles are defined as those suspended in the flue gas stream in contact with mercury-containing flue gas and are characterized by its residence time as short as 0.01 seconds to 30 seconds. The deposited sorbent particles are those adhered onto the surfaces of the boiler system and in direct contact with mercury in flue gas and are characterized by its longer residence time, from 10 seconds up to 10 days. (The upper limit may be determined by the sootblowing cycle and shedding in ductwork.) From a simplistic kinetics point of view, mercury capture by sorbent is expressed as: 
         [0000]      Amount of mercury captured∝(total in-flight particle surface)*(in-flight particle residence time)+(total deposited particle surface)*(deposited particle residence time) 
         [0088]    Of the two groups of carbon sorbent in the boiler system, therefore, the more preferred group is the deposited sorbent particles as they are in contact with mercury in flue gas much longer than are the other group of particles. In accordance with the present invention, the proportion of deposited sorbent particles for the given amount of carbon sorbent injected, the contact surface area of deposited sorbent particles and the residence time of the deposited sorbent particles within the boiler system are all respectively maximized or optimized. 
         [0089]      FIG. 15  shows the contribution of these two groups to mercury capture that were observed in a trial. The initial reduction of mercury from 9 to 2 ug/Nm3 is due to in-flight sorbent and initial sorbent deposit on the reactor wall. As more reactor surface is covered by sorbent, mercury level further goes down to zero at a slower rate as shown in the  FIG. 15 . As soon as the sorbent feeder is turned off, the mercury level is recovered from zero to 4, followed by slow recovery to 6. The recovery from zero to 4 is due to lack of in-flight sorbents, and the recovery from 4 to 6 is due to saturation of deposited sorbent with mercury. 
         [0090]    In a typical coal-fired boiler system, the “backpass devices” that provide a large surface area for sorbent deposition in the desired temperature range of 100 to 1000° F. are the air heaters, the selective catalytic reactors (SCR), the electrostatic precipitator (ESP) entrance nozzles, the ESP collection surfaces, the flue gas ductwork and the fabric filters. In accordance with the present invention, sorbent is injected upstream of any of these devices to coat the surfaces provided by them with sorbent particles. The following are examples of sorbent injection upstream of these devices. 
         [0091]    Air heaters are used for preheating primary and/or secondary air and are an excellent device to provide a large sorbent deposit surface area. In tubular air heaters, cold air flows over a bank of tubes (shell side) through which hot flue gases pass. Mercury sorbents can be injected into flue gases at a location upstream of the air heater tube inlet so that sorbent particles are uniformly distributed across the cross section of the flue gas stream before they enter the heat exchanger tubes. A portion of sorbent particles going through heat exchanger tubes is deposited (or coated) onto the inner surface of tubes, either by Brownian motion or by turbulent diffusion. Particles are held onto the surface mostly by van der Waals force and interact with mercury in flue gases until they are shed off by sootblowing mechanism or simply by flow around them. 
         [0092]    Sorbent injection lances are designed and installed upstream of the inlet with spacing that ensures uniform coating of sorbent particles on the heat exchanger tubes. For maximum utilization of the heat exchanger tube surfaces, it is advantageous if, as shown in  FIG. 16 , a plurality of multiple injection ports  410  are provided to uniformly distribute sorbent particles across the cross section of the flue gas flow. The injection ports  410  may be configured as injection lances and each group of the injection ports  410  are commonly communicated with a respective distribution manifold  412 . Uniform distribution of sorbent particles also ensures good contact between in-flight particles and mercury in flue gases. 
         [0093]    Rotary regenerative air heaters are regenerative heat exchangers with heat exchanger surface elements rotating between hot flue gas duct and cold air ducts. Injection lance systems can be installed upstream of the rotary regenerative air heaters in the flue gas duct to coat the heat exchanger elements uniformly with sorbent particles. 
         [0094]    Sorbent deposition can be enhanced either by modifying the sorbent surfaces or by modifying the surfaces of backpass devices, or both. Sorbent surfaces can be treated with sticky material or its precursors before injection. For example, surfaces of sorbent may be treated with additives such as ammonium bromide, which become sticky as it reacts with sulfur dioxide to form ammonium sulfate. This sticky surface enhances sorbent deposition. 
         [0095]    It can also be advantageous to prepare a slurry mixture of sorbent (solid phase), a liquid phase such as water, and/or other additives (either solid or liquid phase) that enhance mercury chemistry. The slurry is then, as seen in  FIG. 17 , atomized/sprayed into the flue gas, or directly onto surfaces of backpass devices. The liquid phase of the slurry enhances deposition onto backpass surfaces. As the liquid phase of the slurry evaporates, the residual phase (sorbent and/or additives) on the surfaces of backpass devices becomes exposed to flue gas for interaction with mercury. 
         [0096]    Reference is had to  FIG. 18  wherein another enhancement of the process is illustrated wherein the sorbent particles are electrically pre-charged before injection while, downstream of the sorbent injection location, there is provided oppositely charged (or ground) surfaces. The charged sorbent particles then preferentially adhere to these surfaces and interact with mercury for an extended period of time. This also allows selective separation of pre-charged sorbent particles from the non-charged fly ash stream, thereby avoiding any contamination of fly ash stream with sorbent and allowing fly ash utilization for concrete application. 
         [0097]    Another way of avoiding (or minimizing) fly ash contamination while achieving mercury reduction is by injecting sorbent to air side or the neutral zone of rotary regenerative air heaters, rather than flue gas side. In a typical rotary regenerative heater, most of the fly ash particles (&gt;90%) in flue gas pass through air heater. If sorbent particles are injected into flue gas upstream of rotary regenerative heater, most of the sorbent particles will pass through the air heater (in-flight sorbent particles) and only a small portion of the sorbent particles will deposit to the air heater elements (deposited sorbent particles). Most of the injected sorbent particles will participate in the mercury oxidation/capture process for only a short period of time, i.e., 0.01 to 30 seconds, and then end up in ash hoppers of an electrostatic precipitator (ESP) or a baghouse contaminating fly ash stream. 
         [0098]    The contamination of fly ash in ash hoppers can be advantageously minimized by injecting sorbent to the upstream of the air side  502  of the air heater  504  (note that the sectors of this rotor of this rotary regenerative-type air heater cyclically rotate through the air side  502  into which fresh combustion air  506  and the flue gas side  508  into which flue gas flows) or directly into the neutral zone for coating the air heater elements with sorbent. As illustrated in  FIG. 19 , a small portion  510  of the injected sorbent  512  coats the air heater elements  514 , and most of the sorbent particles are entrained by preheated air  516  and eventually end up in the high-temperature burner zone and burn away. 
         [0099]    The sorbent-coated air heater elements  514  in the air-side  502  then rotate into the flue gas side  508  for mercury oxidation and capture. The deposited sorbent particles eventually are dislodged from the element surfaces by sootblowing, entrained by flue gas  518  and end up into the ash hoppers of an ESP or a baghouse. The amount of sorbent into the ash hoppers in this case, however, will be significantly less than that when sorbent is injected to the flue gas side. In this fashion, contamination of fly ash in the ash hoppers is significantly minimized. 
         [0100]    The sorbent that passes through the air-side  502  of the air heater  504  is entrained into the boiler. As the carbonaceous sorbent burns away, any additives in the sorbent are released into flue gas. If the additives are halogen compounds such as chlorine, then the added halogen will participate in the mercury chemistry enhancing mercury oxidation and its capture. 
         [0101]    Combinations of the air-side injection with the flue gas-side injection can be used as well for further control of mercury as is shown in  FIG. 23 . 
         [0102]    The injection of sorbent to the air-side in accordance with the present invention offers a viable mercury control solution to plants with hot-side ESPs as well. A conventional way of mercury control for this configuration is to inject sorbents upstream of the ESP and capture them by the ESP. The technical difficulty in this control method is that the sorbents get to experience the high temperature zone for oxidation, but not the low temperature for mercury capture. The sorbents may participate in the oxidation of mercury but not its capture. 
         [0103]    Sorbent injection to the air-side overcomes this difficulty. Air heaters are located in a temperature range where the kinetics for both oxidation and capture are fast. A combination of flue gas side injection with air-side injection helps control mercury for plant configurations with hot-side ESPs, as is shown in  FIG. 20 . 
         [0104]    The rotation of the air heater elements at a constant speed makes the injection lance system for air-side injection of sorbent simpler than the one for flue gas side injection. The goal of air-side injection is to cover as much surface of air heater elements with sorbents as possible and as uniformly as possible. One may design an injection lance system that covers the whole cross section of the air sector. Since the air heater elements rotate at a constant speed between the flue gas duct and the air duct, however, one can achieve the goal with a simple injection system with a few injection lances extending from the air heater axis to the outer edge in a radial direction. 
         [0105]    An example of the lance system is shown in  FIG. 21 , which is a schematic diagram of the injection of sorbent at the rotary regenerative air heater. Segments A, B, and C are the air-side of the rotary regenerative air heater, whereas D, E and F are the flue gas side. The air in A, B and C is flowing upwards whereas the flue gas in D, E and F is flowing downwards. The heater elements are rotating counterclockwise. In segment C, sorbent has been injected. Some of it is deposited to the heater element surfaces (shown with “x” cross-hatching) and most of it leaves the air heater along with the combustion air. The sorbent-coated heater element enters the flue gas side later and interacts with mercury in flue gas. In this fashion, the sorbent transferred to the flue gas side is only that deposited onto the surfaces. 
         [0106]    Sorbent injection lance system for rotary regenerative air heaters. At time T 0 , air heater segment A is in the air-side of the heater. Injection lance BC is located in this case close to the inlet to the flue gas side as the heater elements rotate counterclockwise. Injection lance BC has multiple nozzles spraying sorbent into general area of line segment BC uniformly. A time t 1 , the segment A approaches the lance BC. At time t 2 , spraying sorbent to the segment A has been completed. Finally at time t 3 , segment A is rotating into the flue gas side. In this fashion, all of the air heater elements are coated with sorbent before they enter the flue gas side. The deposited sorbent on segment A interacts with mercury in flue gas. The flue gas flow is into the page, and the airflow is out of the pages. 
         [0107]    For various reasons, one may opt to generate and/or treat sorbent on site for mercury control. It may be advisable, in connection with the preparation of a small amount of sorbent on site, to ensure the proper environmental control of the undesirable byproducts for the sorbent preparation process. Incorporation of pollution control devices such as scrubbers or particulate control devices dedicated to the sorbent preparation unit makes the on site preparation less economical. A way of overcoming this on-site generation issue is to operatively connect the outlet of on-site generation unit to the upstream of the air-side rotary regenerative heater, as is shown in  FIG. 22 . 
         [0108]    In an on-site generation process, sorbents are generated as well as undesirable byproducts. The byproducts in this case may be any unused additives, intermediate hydrocarbon material produced in the process, solvents or flue gases. As the output stream is directed to the air-side, some sorbents will be deposited onto the air heater element surfaces while the rest escapes the air heater. The escaping stream, which includes most of the byproducts, will be mixed with the combustion air ending up in the combustion zone of the boiler. 
         [0109]    In this way, byproducts from the on-site generation unit undergo high-temperature destruction and are captured by the pollution control devices of the boiler system. 
         [0110]    Thus, it can be understood that the present invention offers the advantages of lower sorbent consumption and costs when employed with an electrostatic precipitator (ESP) and a baghouse, the avoidance of high capital cost equipment (baghouse) downstream of existing ESP, the removal of mercury for cases where no inherent halogen is present in the flue gas (low chlorine fuels), the generation of inactive (lower-activity) carbon in fly ash leading to lower disposal costs and potential use in concrete, and the provision of a cost effective solution to plant configurations with hot-side ESPs. 
         [0111]    While preferred embodiments have been shown and described, various modifications and substitutions may be made thereto without departing from the spirit and scope of the invention. Accordingly, it is to be understood that the present invention has been described by way of illustration and not limitation.