in february and april of 1998 , mcdermott technology , inc . conducted tests , sponsored by the ohio coal development office ( ocdo ) and the u . s . department of energy ( doe ), at its pilot combustion and wet scrubber facility . the purpose of the tests was to study how mercury was affected by conventional pollution control equipment and to investigate various means of improving mercury capture with such conventional equipment . the research focused on the combination of an esp followed by a wet scrubber because this is the system most commonly employed by utilities . referring to the drawings generally , wherein like reference numerals designate the same or functionally similar parts throughout the several drawings , fig1 illustrates a coal - fired utility boiler installation of the type used by utilities in the generation of electric power , generally designated 10 , and which represents one type of industrial process to which the present invention is applicable . in its broadest form , the present invention comprises a method for removing mercury from the flue gas generated during the combustion of fossil fuels or solid wastes through the use of a chelating agent . of course , while the aforementioned coal - fired utility boiler installations are but one example , and the method of the present invention will likely first find commercial application to the removal of mercury from the flue gases produced by such utility boiler installations which combust such fossil fuels , any industrial process using a wet scrubber type of absorber module to purify such flue gases may benefit . such processes could include incineration plants , waste to energy plants , or other industrial processes which generate gaseous products containing mercury . thus for the sake of convenience , the terms industrial gas , flue gas , or just gas will be used in the following discussion to refer to any gas from an industrial process and from which an objectionable component , such as mercury , is to be removed . as illustrated in fig1 and proceeding in the direction of flue gas flow generated during the combustion process , the boiler installation 10 includes a furnace 12 having a gas outlet 14 which conveys flue gases , generally designated 16 , to an air heater 18 used to preheat incoming air 20 for combustion . pulverizers 22 grind a fossil fuel 24 ( e . g ., coal ) to a desired fineness and the pulverized coal 24 is conveyed via burners 25 into the furnace 12 where it is burned to release heat used to generate steam for use by a steam turbine - electric generator ( not shown ). flue gas 16 produced by the combustion process are conveyed through the gas outlet 14 to the air heater 18 and thence to various types of downstream flue gas cleanup equipment . the flue gas cleanup equipment may comprise a fabric filter or , as shown , an electrostatic precipitator ( esp ) 26 which removes particulates from the flue gas 16 . a flue 28 downstream of the esp 26 conveys the flue gas 16 to a wet scrubber absorber module 30 which is used to remove sulfur dioxide and other contaminants from the flue gas 16 . flue gas 16 exiting from the wet scrubber absorber module or , simply , the wet scrubber 30 , is conveyed to a stack 32 and exhausted to atmosphere . forced draft fans 34 and induced draft fans 36 are used to propel the air 20 , fuel 24 , and flue gases 16 through the installation 10 . for further details of various aspects of such installations 10 , the reader is referred to steam its generation and use , 40th ed ., stultz and kitto , eds ., copyright © 1992 the babcock & amp ; wilcox company , particularly to chapter 35 — sulfur dioxide control , the text of which is hereby incorporated by reference as though fully set forth herein . while the aforementioned steam reference contains a description of one form of wet scrubber 30 produced by the babcock & amp ; wilcox company ( b & amp ; w ) and to which the present invention is applicable , the present invention is not limited to such b & amp ; w wet scrubber designs . persons skilled in the art will appreciate that the principles of the present invention apply equally well to other types of wet scrubber designs , available from other manufacturers . referring again generally to fig1 and to fig2 and 3 in particular , it has been found that an esp affects the process chemistry so that hg + 2 is converted to hg 0 within a downstream wet scrubber . fig2 shows the vapor - phase mercury concentration of both hg + 2 and hg 0 measured at the inlet of a pilot wet scrubber ( not shown ) at the mcdermott technology , inc . alliance research center in alliance , ohio for the cases when the esp was operated normally (“ esp baseline test ”) and when it was operated at high voltage levels (“ esp high power test ”). in each bar graph of fig2 and 3 , the hg 0 concentration is designated 200 , while the hg + 2 concentration is designated 400 . fig2 clearly shows that the electric field in the esp has a negative impact on the mercury collection efficiency of the wet scrubber , but does not directly affect mercury speciation of the flue gas . the relative amount of the different mercury species at the wet scrubber inlet is the same for both cases . however , the amount of hg 0 greatly increases across the wet scrubber for the high power test . this indicates that the electric field affects some component of the flue gas which , in turn , has a negative impact on the wet scrubber chemistry . since hg is present in such small quantities , it is likely that the affected component is also present in small quantities . a possible mechanism that explains the observed results is presented below . in this scenario , the electric field within the esp creates ozone ( this is known to occur ). the ozone then destroys hydrogen sulfide ( h 2 s ), which is present in small quantities , and is thus unavailable to capture hg + 2 as mercuric sulfide ( hgs ). hg + 2 is subsequently converted to hg 0 by some transition metal . for example , in the case of iron ( fe ): h 2 s + o 3 → h 2 o + so 2 ozone created by the strong electrical field destroys h 2 s h 2 s → 2h + + s − 2 h 2 s dissociates in the wet scrubber s − 2 + hg + 2 → hgs h 2 s contributes to hg removal 2fe + 2 + hg + 2 → 2fe + 3 + hg 0 fe + 2 reduces hg + 2 to hg 0 . the present invention is believed to block the action of transition metals by the use of a chelating agent , particularly ethylenediaminetetraacetic acid ( edta ). as set forth below , one possible mechanism could be as follows : 2fe + 2 + edta − 4 →[ 2fe ( edta )] sequesters fe + 2 species and prevents it from reducing hg + 2 . the use and effect of chelating reagents are well known ; however , to the inventor &# 39 ; s knowledge they have never been applied in this industry for the purpose of improving mercury capture within conventional wet scrubbers 30 . the present invention involves the discovery that chelating agents can be used to unexpectedly improve mercury capture in conventional wet scrubbers 30 located downstream ( with respect to a direction of flue gas flow 16 ) of an esp 26 . the exact mechanism by which an esp 26 affects the process chemistry and causes additional hg + 2 to be converted to hg 0 within the wet scrubber 30 is not important . indeed , it is possible that the chelating agent may be acting directly on the mercury species , as well , alone or in combination with actions on the transition metals as postulated above . what is important , however , is that , by some mechanism , hg + 2 is being converted to hg 0 and that a chelating agent can be used to prevent it . the most likely mechanism by which this occurs probably involves a transition metal and , most likely , iron . chelating agents are known to sequester transition metals , however , in the thick chemical soup that describes wet scrubber slurry , the action of a chelating agent could not be predicted . the chemistry of limestone scrubbing is very complicated due to the many species present at equilibrium . the flue gas and limestone , plus fly ash from coal - burning boilers , each contribute several constituents that affect the chemical makeup of the system . so 2 , so 3 , co 2 , o 2 , no and no 2 originate from the flue gas ; k , cl , fe , and other chemicals arrive with the fly ash ; and the limestone contains ca , mg and several other minor constituents such as na and k . therefore , a chelating agent , ethylenediaminetetraacetic acid ( edta ), was added to the reaction tank of a pilot - scale wet scrubber , and mercury concentration was measured at the inlet and outlet of the wet scrubber . the test was conducted at the mcdermott technology , inc ., pilot - scale , clean environment development facility ( cedf ) operated at a nominal heat input of approximately 100 million btu / hr . pulverized coal , ground to approximately 75 % less than 200 mesh , was burned in a b & amp ; w low - nox , plug - in burner at a coal flow rate of approximately 4 tons per hour to generate flue gas for the test . after passing through an esp , the flue gas flowed through a wet scrubber comprising a slurry recirculation tank , a reagent feed system , and a mist eliminator wash system all of known design . pulverized limestone was mixed with make - up water in a reagent feed tank to maintain a solids content of the recirculating slurry at about 12 - 15 %. ten pounds of a chelating agent , edta , were added to the wet scrubber slurry recirculation tank , containing 1 , 200 gallons of slurry , to produce a solution containing approximately 2 moles chelating agent per estimated mole of transition metal , such as iron , in the wet scrubber slurry or approximately twice the amount needed based on stoichiometry . this solution was introduced into the scrubber at a rate of about 120 gallons per minute per 1000 actual cubic feet per minute of mercury - containing flue gas . fig3 shows how edta affected the wet scrubber chemistry . before edta was added , a large portion of hg + 2 was being converted to hg 0 . after edta was added , the concentration of hg 0 at the wet scrubber outlet was reduced to levels similar to that at the wet scrubber inlet that indicates no new hg 0 was formed in the wet scrubber . fig3 also shows that edta did not affect the normal removal efficiency of hg + 2 . the net result was that total mercury removal across the wet scrubber improved from 46 % to 73 % with the introduction of edta . referring again to fig1 the method according to the present invention can be easily adapted to an existing installation 10 using a wet scrubber 30 . the preferred chelating agent , generally designated 50 , according to the present invention is edta . other suitable chelating agents include , but are not limited to : hydroxyethylenediaminetetraacetic acid ( hedta ), diethylenetriaminepentaacetic acid ( dtpa or pentetic acid ), or nitrilotriacetic acid ( nta ). the salt or acid forms of the chelating agents are suitable for use in the present invention . the chelating agent 50 could be provided from a chelating feed system , generally designated 52 , via a line 54 into the wet scrubber slurry 56 contained in a lower portion of the wet scrubber 30 . recirculating pumps 59 continuously pump the wet scrubber slurry 56 from the lower portion to upper headers 57 located within an upper portion of the wet scrubber 30 which spray slurry 56 into the flue gas 16 being treated by the wet scrubber 30 . if desired , the method according to the present invention may comprise determining the concentration of oxidized ( hg + 2 ) and elemental ( hg 0 ) forms of mercury in the flue gases 16 entering and exiting from the wet scrubber 30 and supplying the chelating agent 50 into the slurry 56 being recirculated therein in an amount sufficient to reduce the degree to which at least one transition metal converts the hg + 2 into the hg 0 form based upon such determination . measurements from mercury concentration sensors 58 and 60 located at the exit , and inlet , respectively , of the wet scrubber 30 may be employed for this purpose , and to determine the effectiveness of chelating agent 50 addition ; signals indicative of these measurements could be sent via the dashed lines as shown to the chelating feed system 52 to automatically control the amount of chelating agent 50 supplied . alternatively , instead of a system employing sensors , batch sampling at the exit and / or inlet of the wet scrubber 30 could be used to determine the hg levels , and the amount of chelating agent 50 supplied would be based on such batch samples . still further , it might be desirable to merely ensure that an excess of chelating agent 50 is provided at all times to ensure that a desired level of hg removal is obtained . similarly , the method according to the present invention may comprise determining the amount of the at least one transition metal in the wet scrubber slurry and supplying the chelating agent 50 into the slurry in an amount sufficient to reduce the degree to which the at least one transition metal converts the hg + 2 into the hg 0 form based upon such determination . alternatively , a set point could be established based on calculated or historical data and set manually . for all three cases described immediately above , operator control means 64 associated with the chelating feed system 52 could be used to establish setpoints 66 , mode of operation , or perform manual control of the chelating feed system 52 as desired . the signals indicative of the measurements from the aforementioned mercury concentration sensors located at the exit 58 and inlet 60 of the wet scrubber 30 may also be sent directly to the operator control means 64 ( via dashed lines as shown ) which could then be used to communicate with and / or control the chelating feed system 52 via lines 68 . chelating agent 50 may be added directly to slurry 56 and / or slurry 56 may be drawn out of scrubber 30 via line 62 with agent 50 being mixed in chelating feed system 52 with the mixture of slurry 56 and chelating agent 50 subsequently reintroduced to scrubber 30 via line 54 . this invention thus generally applies to the process whereby a chelating agent 50 is added to a wet scrubber system 30 for the purpose of facilitating the removal of mercury . as described above , there are a wide variety of chelating agents and methods to introduce them into the wet scrubber 30 . a person skilled in this art can determine the most effective and economical agent , as well as what quantities to use , and the most effective means of delivery . in any application , the critical feature is to ensure supplying the chelating agent into the slurry or liquid used to scrub the flue gases 16 in an amount sufficient to at least reduce the degree to which the at least one transition metal converts the hg 0 into the hg + 2 form . similarly , for example , the particular means by which the chelating agent 50 is provided to the wet scrubber 30 is relatively unimportant , so long as some consistent and measurable means are employed so the process can be employed . the chelating agent 50 may be conveyed to the wet scrubber via pneumatic , liquid , or gravity means and introduced continuously or in batch form at desired intervals . alternatively , the chelating agent 50 could be injected upstream of the wet scrubber 30 . one or more chelating agents 50 may be employed as desired , depending upon the relative economics and the particular transition metal which is determined to be of interest and which is to be sequestered by the chelating agent . the above - identified pilot - scale testing demonstrates that a method and system for implementing same according to the present invention is feasible , effective , and practical . to the inventor &# 39 ; s knowledge , no prior art exists for enhanced mercury removal across wet scrubber systems using chemical additives . fig3 shows that a chelating agent 50 can be used to improve mercury removal efficiency across a wet scrubber 30 for those systems that use an esp 26 for particulate control . the advantages of this invention are several : 1 . chelating agents 50 are well known , widely available , and relatively inexpensive . 2 . conventional wet scrubbers 30 can be used . that is , no new pollution control equipment need be installed to control mercury , except a small chemical feed system 52 ( as illustrated in fig1 ) for introducing the chelating agent 50 . 3 . the invention may improve the so 2 removal efficiency of the wet scrubber 30 as well . in the tests described above , so 2 removal increased from 95 . 6 % to 97 . 9 % when edta was added . although this may not seem like a big improvement when presented in terms of percent removal , it represents a 24 % increase in transfer units from ( 3 . 12 to 3 . 86 ) which is very significant . this is an unexpected result , and a result that would make the invention even more attractive to potential customers . 4 . this invention applies to the majority of flue gas desulfurization systems used by electric utilities and is not limited in application to any particular flue gas desulfurization system or wet scrubber design . while a specific embodiment of the invention has been shown and described in detail to illustrate the application of the principles of the invention , it will be understood that the invention may be embodied otherwise without departing from such principles . accordingly , all such embodiments and applications of the present invention properly fall within the scope and equivalents of the following claims .