Patent Abstract:
A flue gas desulfurization process and system that utilize ammonia as a reactant, and in which any hydrogen sulfide and/or mercaptans within the ammonia are separated during the desulfurization process so as to prevent their release into the atmosphere. The process and system entail absorbing acidic gases from a flue gas with a scrubbing media containing ammonium sulfate to produce a stream of scrubbed flue gas, collecting the scrubbing media containing the absorbed acidic gases, injecting into the collected scrubbing media a source of ammonia that is laden with hydrogen sulfide and/or mercaptans so that the injected ammonia is absorbed into and reacted with the collected scrubbing media, stripping the hydrogen sulfide and/or mercaptans from the collected scrubbing media by causing the hydrogen sulfide and/or mercaptans to exit the collected scrubbing media as stripped gases, and collecting the stripped gases without allowing the stripped gases to enter the stream of scrubbed flue gas.

Full Description:
CROSS REFERENCE TO RELATED APPLICATIONS 
       [0001]    This application claims the benefit of U.S. Provisional Application No. 60/914,081, filed Apr. 26, 2007, the contents of which are incorporated herein by reference. 
     
    
     BACKGROUND OF THE INVENTION 
       [0002]    The present invention generally relates to processes and systems for removing acidic gases from flue gases produced by power generation, industrial, and other facilities. More particularly, this invention is directed to flue gas desulfurization (FGD) processes and systems that utilize ammonia to capture sulfur dioxide and produce ammonium sulfate, with the further capability of preventing or at least reducing the release of hydrogen sulfide and/or mercaptans into a scrubbed flue gas stream produced by such processes and systems. 
         [0003]    Acidic gases, including sulfur dioxide (SO 2 ), hydrogen chloride (HCl) and hydrogen fluoride (HF), are known to be hazardous to the environment, and as a result their emission into the atmosphere is closely regulated by clean air statutes. For the removal of acidic gases from flue gases produced by utility and industrial plants, gas-liquid scrubbers (contactors, absorbers, etc.), are widely employed. Scrubbers generally employ a liquid-containing media that is brought into intimate contact with a flue gas to remove acidic gases by absorption. The process by which acidic gases are removed from flue gases in this manner is generally referred to as wet flue gas desulfurization (wet FGD). 
         [0004]    The cleansing action produced by scrubbers is generally derived from the passage of a flue gas through a tower cocurrently or countercurrently to a descending liquid medium. Calcium-based slurries, sodium-based solutions and ammonia-based solutions are typical alkaline scrubbing media used in flue gas scrubbing operations. The cleansed gases are allowed to exit the tower, typically passing through a mist eliminator to atmosphere. The liquid medium and its absorbed gases are collected in a tank, typically at the bottom of the tower, where the absorbed gases are reacted to form byproducts that are useful or at least not harmful to the environment. While scrubbers utilizing calcium-based slurries generally perform satisfactorily, their operation results in the production of large quantities of wastes or gypsum, the latter having only nominal commercial value. 
         [0005]    In contrast, ammonia-based scrubbing processes have been used to produce a more valuable ammonium sulfate fertilizer, as taught by U.S. Pat. Nos. 4,690,807 and 5,362,458, each of which are assigned to the assignee of the present invention and incorporated herein by reference. In these processes (also known as ammonium sulfate flue gas desulfurization, or AS FGD), the scrubbing solution is accumulated in a tank where the absorbed sulfur dioxide reacts with dissolved ammonia (NH 3 ) to form ammonium sulfite ((NH 4 ) 2 SO 3 ) and ammonium bisulfite (NH 4 HSO 3 ), which are oxidized in the presence of sufficient oxygen to form ammonium sulfate ((NH 4 ) 2 SO 4 ) and ammonium bisulfate (NH 4 HSO 4 ), the latter of which reacts with ammonia to form additional ammonium sulfate. A portion of the ammonium sulfate solution and/or ammonium sulfate crystals that form in the solution can then be drawn off to yield the desired byproduct of this reaction. 
         [0006]    Ammonia produced from sour water in refinery, tar sands and other similar applications typically contains low concentrations of hydrogen sulfide (H 2 S) and mercaptans (or thiols, which are compounds that contain the functional group composed of a sulfur atom and a hydrogen atom (—SH)). When the ammonia is used in an ammonium sulfate FGD system to capture sulfur dioxide, the hydrogen sulfide and mercaptans are stripped from the ammonia because of their volatility in ammonium sulfate, and thereafter become entrained with the flue gas. Scrubbed flue gases that exit the FGD system contain the entrained hydrogen sulfide and mercaptans which, in addition to being air pollutants, can contribute an undesirable odor to the FGD emissions. 
         [0007]    Current technologies employed to purify ammonia and separate it from hydrogen sulfide and mercaptans are expensive capital-intensive processes, and consume considerable amounts of energy. As such, it would be desirable if an improved process were available that was capable of greatly reducing the amounts of hydrogen sulfide and mercaptans released from AS FGD systems, while also avoiding the disadvantages of prior art processes. 
       BRIEF SUMMARY OF THE INVENTION 
       [0008]    The present invention provides a flue gas desulfurization process and system that utilize ammonia as a reactant, and in which any hydrogen sulfide and/or mercaptans within the ammonia are separated during the desulfurization process so as to prevent their release into the atmosphere. 
         [0009]    According to a first aspect of the invention, the process includes absorbing acidic gases from a flue gas with a scrubbing media containing ammonium sulfate to produce a stream of scrubbed flue gas, collecting the scrubbing media containing the absorbed acidic gases, injecting into the collected scrubbing media a source of ammonia that is laden with hydrogen sulfide and/or mercaptans so that the injected ammonia is absorbed into and reacted with the collected scrubbing media, stripping the hydrogen sulfide and/or mercaptans from the collected scrubbing media by causing the hydrogen sulfide and/or mercaptans to exit the collected scrubbing media as stripped gases, and collecting the stripped gases without allowing the stripped gases to enter the stream of scrubbed flue gas. 
         [0010]    According to a second aspect of the invention, the system includes means for absorbing acidic gases from a flue gas with a scrubbing media containing ammonium sulfate to produce a stream of scrubbed flue gas, means for collecting the scrubbing media containing the absorbed acidic gases, means for injecting into the collected scrubbing media a source of ammonia that is laden with hydrogen sulfide and/or mercaptans so that the injected ammonia is absorbed into and reacted with the collected scrubbing media, means for stripping the hydrogen sulfide and/or mercaptans from the collected scrubbing media by causing the hydrogen sulfide and/or mercaptans to exit the collected scrubbing media as stripped gases, and means for collecting the stripped gases without allowing the stripped gases to enter the stream of scrubbed flue gas. 
         [0011]    In flue gas desulfurization processes and systems of this invention, the scrubbing media can be collected in a tank located, and the hydrogen sulfide and/or mercaptans can be stripped from the scrubbing media in the tank or in a separate vessel fluidically connected to the tank. In either case, it can be seen that a significant advantage of this invention is that ammonia containing undesired levels of hydrogen sulfide and mercaptans can be used in a desulfurization process, but with a greatly reduced risk of releasing gaseous hydrogen sulfide and mercaptans into the atmosphere along with the scrubbed flue gas. As such, the present invention is capable of avoiding disadvantages associated with current technologies used to purify ammonia and separate it from hydrogen sulfide and mercaptans prior to its use in an ammonium sulfate-based flue gas desulfurization process. 
         [0012]    Other objects and advantages of this invention will be better appreciated from the following detailed description. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS  
         [0013]      FIG. 1  is a schematic representation of a flue gas scrubbing apparatus configured for in situ removal of hydrogen sulfide and mercaptans in accordance with a first embodiment of this invention. 
           [0014]      FIG. 2  is a schematic representation of a flue gas scrubbing apparatus equipped with a dedicated stripping tank for removal of hydrogen sulfide and mercaptans in accordance with a second embodiment of this invention. 
       
    
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0015]      FIGS. 1 and 2  represent two embodiments of ammonia-based FGD systems  10  and  100  that allow the use of ammonia containing hydrogen sulfide and/or mercaptans. The systems  10  and  100  employ a relatively low cost process for reducing the release of hydrogen sulfide and mercaptans by separating and capturing these pollutants after they are stripped from the contact media used in the AS FGD process. The process can be integrated into an otherwise conventional AS FGD system and operation through relatively uncomplicated modifications to the AS FGD system, incurring minimal capital investment and energy consumption.  FIGS. 1 and 2  are drawn for purposes of clarity when viewed in combination with the following description, and therefore are not necessarily to scale. 
         [0016]    The invention utilizes the fact that ammonia is soluble in water and acidic solutions, while the solubilities of hydrogen sulfide and mercaptans in water and acidic solutions are lower. Ammonium sulfate scrubbing media (including solutions and slurries, depending on solids content) accumulated in AS FGD systems after the absorption of sulfur dioxide from flue gases are acidic, with pH levels typically in a range of about 4 to about 6. When ammonia laden with hydrogen sulfide and/or mercaptans is introduced into the ammonium sulfate media, the ammonia is readily absorbed and reacts with the absorbed sulfur dioxide, while the hydrogen sulfide and mercaptans are stripped from the liquid to the gas phase. In typical FGD systems, the reaction tank in which the scrubbing media is accumulated is often open at its upper end. Air that has been injected into the scrubbing media to react and form ammonium sulfate mixes with the stripped hydrogen sulfide and mercaptans, and the resulting mixture is then able to mix with the scrubbed flue gases, producing an undesirable odor and emission of harmful species. 
         [0017]    The present invention reduces the release of hydrogen sulfide and mercaptans by adding the hydrogen sulfide and mercaptans-laden ammonia to the ammonium sulfate media in such a way that stripping of hydrogen sulfide and mercaptans occurs in a confined zone, thus avoiding the mixing of hydrogen sulfide and mercaptans gases with the scrubbed flue gas. The gaseous hydrogen sulfide and mercaptans are then diverted away from the FGD system, and can be captured, incinerated, or otherwise prevented from release into the atmosphere. 
         [0018]    In accordance with the above, the AS FGD systems  10  and  100  represented in  FIGS. 1 and 2  are each configured to separate hydrogen sulfide and mercaptans and prevent the contamination of a flue gas. The FGD systems  10  and  100  are generally represented as being of a type that scrubs flue gases produced by the burning of fossil fuels or another process that results in the flue gas containing acidic gases, such as sulfur dioxide, hydrogen chloride and/or hydrogen fluoride, as well as particulate matter, nitrogen oxides (NOx), etc. Referring to  FIG. 1 , the conventional components of the FGD system  10  include an absorber tower  14  having a contact zone  16  in which an ammonium sulfate scrubbing media (e.g., solution or slurry)  26  is brought into contact with a flue gas that enters the FGD system  10  through an inlet duct  12 . The scrubbing media  26  is shown as being collected in a tank  18  located at the bottom of the tower  14 . The media  26  is drawn from the tank  18  with a pump  20  and then delivered through a pipe  22  to the contact zone  16 , where the scrubbing media  26  is dispersed with spray nozzles  24  or another suitable delivery device. After being scrubbed by the scrubbing media  26 , the resulting scrubbed stream of flue gas flows upward, typically through a mist eliminator and/or other equipment (not shown), and is eventually released to atmosphere through a chimney or other suitable structure. As with many existing wet flue gas desulfurization facilities, the FGD system  10  is equipped for in situ forced oxidation of the scrubbing media  26  that has collected in the tank  18 . In  FIG. 1 , a source  60  of oxygen, such as air or another oxygen-containing gas (hereinafter referred to as air for convenience), is represented as being introduced into the tank  18  with a sparger  28  connected to a suitable source  30 . The air is typically injected near the bottom of the tank  18 , so that the gas migrates upward as bubbles  48  through the scrubbing media  26  in the tank  18 . In this manner, reaction products produced by contacting the acidic gases of the flue gas with the scrubbing media  26  are oxidized by the oxygen in the sparged air to preferably yield ammonium sulfate as a useful fertilizer byproduct. 
         [0019]    As taught by commonly-assigned U.S. Pat. Nos. 4,690,807 and 5,362,458, following absorption of the acidic gases present in a flue gas, the ammonium sulfate media  26  collected in the tank  18  has a relatively low pH, for example, about 4 to about 6. Aqueous ammonia (ammonium hydroxide, NH 4 OH) or another source of ammonia  31  is introduced into the collected media  26 , such as with a second sparger  32 , typically near the top of the reaction tank  18  and preferably a meter or so below the surface of the scrubbing media  26  in the tank  18 . The absorbed sulfur dioxide reacts with the ammonia to form ammonium sulfite (NH 4 ) 2 SO 3  and ammonium bisulfite (NH 4 HSO 3 ), which are then oxidized in the presence of sufficient oxygen (introduced by the sparger  28 ) to form precipitates of ammonium sulfate and ammonium bisulfate (NH 4 HSO 4 ). Ammonium bisulfate undergoes a second reaction with the injected ammonia to form additional ammonium sulfate precipitate. A portion of the ammonium sulfate media  26  is typically removed from the tank  18  and dewatered with a suitable dewatering device (not shown) to precipitate ammonium sulfate, which can then be sold as a valuable fertilizer. If hydrogen chloride and hydrogen fluoride were present in the flue gas, as is typically the case with flue gas produced by the combustion of coal, these acidic gases are also captured to form ammonium chloride and ammonium fluoride, which can be removed in the same manner. Further details regarding the desulfurization of flue gases can be obtained in the prior art, including the above-noted U.S. Pat. Nos. 4,690,807 and 5,362,458, and therefore will not be discussed in any further detail here. 
         [0020]    Any hydrogen sulfide and mercaptans present in the ammonia introduced with the sparger  32  will also be present in the scrubbing media  26  collected in the tank  18 . A portion of the absorbed hydrogen sulfide and mercaptans is likely to be stripped from the scrubbing media  26  by the action of the oxidation air introduced into the scrubbing media  26  by the sparger  28 , with the result that the oxidation air released from the surface of the scrubbing media  26  in the tank  18  (as represented by the arrows in  FIG. 1 ) will be accompanied by gaseous hydrogen sulfide and mercaptans. To inhibit mixing of the oxidation air and gaseous hydrogen sulfide and mercaptans released from the scrubbing media  26  with the flue gas traveling through the contact zone  16 ,  FIG. 1  shows a divider  34  separating the reaction tank  18  from the contact zone  16 . The divider  34  is represented as having an inverted conical shape, with a passage  36  located at its central lowermost extent through which the scrubbing media  26  can enter the tank  18  following contact with the flue gas in the contact zone  16 . The passage  36  is represented as being entirely open at its upper limit  38  and closed at its lower limit  40 , which is submerged below the surface of the scrubbing media  26  in the tank  18 . The passage  36  further has one or more submerged peripheral openings  42  located at its perimeter near its closed lower limit  40 , and through which the scrubbing media  26  is able to flow directly into the collected media  26  within the tank  18 . 
         [0021]    The inverted conical shape of the divider  34  and the size and configuration of the passage  36  cause the oxidation air and gaseous hydrogen sulfide and mercaptans released from the scrubbing media  26  to flow toward the perimeter of the tank  18  above the scrubbing media  26 , and into a confined zone  44  bounded by the surface of the scrubbing media  26 , the divider  34 , the exterior of the passage  36 , and the exposed wall of the tank  18  between the surface of the scrubbing media  26  and the divider  34 . From the confined zone  44 , the gaseous hydrogen sulfide and mercaptans can be diverted through a pipe  46  or other suitable structure and subsequently captured, incinerated, or otherwise disposed of or processed in any desirable manner. 
         [0022]    The FGD system  100  represented in  FIG. 2  provides an alternative configuration capable of removing hydrogen sulfide and mercaptans brought into the system  100  with ammonia. Because of the similarities in their construction and operation, consistent reference numbers are used to identify functionally similar structures in  FIGS. 1 and 2 . The system  100  of  FIG. 2  primarily differs from that of  FIG. 1  by providing a dedicated hydrogen sulfide and mercaptans stripping vessel  50  in close proximity to the tower  14 , the latter of which again includes a contact zone  16  and reaction tank  18  whose purposes are essentially the same as described for the embodiment of  FIG. 1 . The reaction tank  18  and the stripping vessel  50  are connected near their lower ends via a passage  62  that provides for equalization of the liquid levels in the tank  18  and vessel  50 . 
         [0023]    As in the system  10  of  FIG. 1 , the system  100  of  FIG. 2  utilizes a pump  20  to draw the ammonium sulfate scrubbing media  26  from the reaction tank  18 , and then deliver the drawn media  26  through a pipe  22  to nozzles  24  located in the contact zone  16  of the tower  14 . In addition, a portion of the scrubbing media  26  is shown as being delivered by the pump  20  through a second pipe  52  to the stripping vessel  50 , where the scrubbing media  26  is injected into the scrubbing media  26  within the vessel  50  at some distance below the surface of the scrubbing media  26  in the vessel  50 . For the reasons described in reference to the system  10  of  FIG. 1 , air is preferably injected with a sparger  28  into the scrubbing media  26  near the bottom of the reaction tank  18 . Air is also injected into the stripping vessel  50  with a sparger  58 , preferably at roughly the same elevation as the air injection site in the reaction tank  18 . Instead of being injected into the reaction tank  18  as done in  FIG. 1 , ammonia (and any hydrogen sulfide and/or mercaptans contained therein) is drawn from a suitable source  31  and injected with a sparger  32  into the stripping vessel  50 . Similar to  FIG. 1 , the ammonia is preferably injected near the top of the vessel  50 , for example, a meter or so below the surface of the scrubbing media  26  in the vessel  50 , and preferably below the location where the scrubbing media  26  is introduced into the vessel  50 . Alternatively, the ammonia laden with hydrogen sulfide and mercaptans can be injected into the pipe  52 , so as to be mixed and delivered with the recycled media  26  to the vessel  50 . 
         [0024]    The injected ammonia is captured by the low-pH media  26  as it flows downwardly through the stripping vessel  50  toward the tank  18 . In so doing, the media  26  within the vessel  50  flows counter-currently to the air injected into the vessel  50  with the sparger  58 . Simultaneously, the hydrogen sulfide and mercaptans introduced with the ammonia into the vessel  50  are stripped out of the scrubbing media  26  by the upward flow of bubbles  48  from the air sparger  58 . Air and the stripped gaseous hydrogen sulfide and mercaptans exit the scrubbing media  26  and enter the confined zone  44  between the surface of the scrubbing media  26  in the vessel  50  and the top of the vessel  50 , and from there can be diverted through a pipe  46  or other suitable structure and subsequently captured, incinerated, or otherwise disposed of or processed in any desirable manner. The pH of the scrubbing media  26  increases as it flows downward through the stripping vessel  50  as a result of the captured ammonia, and is returned by gravity to the reaction tank  18  through the passage  62 . 
         [0025]    In view of the above, it can be appreciated that the systems  10  and  100  effectively isolate and remove hydrogen sulfide and mercaptans that are typically present in sources of ammonia (e.g., aqueous ammonia) used in AS FGD processes, and otherwise escape into the atmosphere with the scrubbed flue gases. As such, the invention avoids the disadvantages of current technologies that seek to avoid hydrogen sulfide and mercaptans by purifying ammonia using expensive and capital-intensive processes. 
         [0026]    While the invention has been described in terms of specific embodiments, it is apparent that other forms could be adopted by one skilled in the art. For example, the physical configuration of the systems  10  and  100  could differ from that shown, and components other than those noted could be used, including devices other than spargers and nozzles that are adequately capable of dispensing fluids including air, ammonia, and scrubbing media in a suitable manner. Therefore, the scope of the invention is to be limited only by the following claims.

Technology Classification (CPC): 1