Flue gas desulfurization is commonly known as FGD and is the technology used for removing sulfur dioxide (SO2) from the exhaust combustion flue gases of power plants that burn coal or oil to produce steam for the turbines that drive their electricity generators. The most common types of FGD contact the flue gases with an alkaline sorbent such as lime or limestone.
As sulfur dioxide is responsible for acid rain formation, stringent environmental protection regulations have been enacted in many countries to limit the amount of sulfur dioxide emissions from power plants and other industrial facilities.
Prior to the advent of strict environmental protection regulations, tall flue gas stacks (i.e., chimneys) were built to disperse rather than remove the sulfur dioxide emissions. However, that only led to the transport of the emissions to other regions. For that reason, a number of countries also have regulations limiting the height of flue gas stacks.
For a typical conventional coal-fired power plant, FGD technology will remove up to 99 percent of the SO2 in the flue gases.
Methods for removing sulfur dioxide (SO2) from flue gases have been studied for over 150 years. Early concepts useful for flue gas desulfurization appear to have germinated in 1850 in England.
With the construction of large-scale power plants in England in the 1920s, the problems associated with large volumes of sulfur dioxide emissions began to concern the public. The problem did not receive much attention until 1929, when the British government upheld the claim of a landowner against the Barton Electricity Works for damages to his land resulting from sulfur dioxide emissions. Shortly thereafter a press campaign was launched against the erection of power plants within the confines of London. This led to the imposition of sulfur dioxide controls on all such power plants.
During this period, major FGD installations went into operation in England at three power plants. The first one began operation at the Battersea Station in London in 1931. In 1935, the second one went into service at the Swansea Power Station. The third one was installed in 1938 at the Fulham Power Station. All three installations were abandoned during World War II.
Large-scale FGD units did not reappear in commercial operation until the 1970s, and most of the activity occurred in the United States and Japan. As of June 1973, there were 42 FGD units, ranging in size from 5 to 250 megawatts (MW), in operation: 36 in Japan and 6 in the United States.
As of about 1999-2000, there were 678 FGD units operating worldwide (in 27 countries) producing a total of about 229 gigawatts (GW). About 45% of that FGD capacity was in the United States, 24% in Germany, 11% in Japan and 20% in various other countries. Approximately 79% of the units, representing about 199 gigawatts of capacity, were using lime or limestone wet scrubbing. About 18% (or 25 gigawatts) utilized spray-dry scrubbers or dry sorbent injection systems.
SO2 is an acidic gas. Therefore, the most common large-scale FGD systems use an alkaline sorbent such as lime or limestone to neutralize and remove the SO2 from the flue gas. Since lime and limestone are not soluble in water, they are used either in the form of an aqueous slurry or in a dry, powdered form.
When using an aqueous slurry of sorbent, the FGD system is referred to as a wet scrubber. When using a dry, powdered sorbent, the system is referred to as a dry system. An intermediate or semi-dry system is referred to as a spray-dry system.
When wet scrubbing with a Ca(OH)2 (lime) slurry, the reaction also produces CaSO3 (calcium sulfite) and can be expressed as:
Ca(OH)2 (solid) + SO2 (gas) ⇒ CaSO3 (solid) + H2O (liquid)
When wet scrubbing with a Mg(OH)2 (magnesium hydroxide) slurry, the reaction produces MgSO3 (magnesium sulfite) and can be expressed as:
Mg(OH)2 (solid) + SO2 (gas) ⇒ MgSO3 (solid) + H2O (liquid)
Some FGD systems go a step further and oxidize the CaSO3 (calcium sulfite) to produce marketable CaSO4 · 2H2O (gypsum):
CaSO3 (solid) + ½ O2 (gas) + 2H2O (liquid) ⇒ CaSO4 · 2H2O (solid)
Aqueous solutions of sodium hydroxide (NaOH), known as caustic soda or simply caustic, may also be used to neutralize and remove SO2 from flue gases. However, caustic soda is limited to small-scale FGD systems, mostly in industrial facilities other than power plants because it is more expensive than lime. It has the advantage that it forms an aqueous solution rather than a slurry and that makes it easier to operate. It produces a solution of sodium sulfite or sodium bisulfite (depending on the pH), or sodium sulfate that must be disposed of. This is not a problem in a paper mill for example, where the solution can be recycled and reused within the paper mill.
Types of FGD systems
The major types of large-scale, power plant FGD systems include spray towers, spray dryers and dry sorbent injection systems.
There are various types of wet scrubbers. For example, spray towers, venturi scrubbers, packed towers and trayed towers. Slurries would cause serious erosion problems in a venturi scrubber because of the high speeds at the throat of the venturi section. Packed towers or trayed towers would plug up if handling slurries. For handling slurries, the spray tower is a good choice and it is in fact a commonly used choice in large-scale FGD systems.
As shown in the adjacent location drawing, spray towers are used downstream of the particulate removal equipment (electrostatic precipitator or filter baghouse) where the flue gas then contains very little, if any, combustion fly ash. In a spray tower system, the sorbent slurry is simply injected via spray nozzles into a vertical tower where the slurry droplets are contacted with the upflowing flue gas.
Part of the water in the slurry is evaporated by the hot flue gas and the flue gas becomes saturated with water vapor.
The SO2 dissolves into the slurry droplets and reacts with the alkaline sorbent particles. The slurry falls to the bottom of the spray tower and is sent to a reaction tank where the reaction is completed and a neutral salt is formed. In a regenerable system, the residual slurry is recycled back for reuse in the spray tower. In a once-through system, the residual slurry is dewatered and either disposed of or oxidized to CaSO4 · 2H2O and sold as a by-product gypsum.
Spray-dryers are used upstream of the particulate removal equipment (electrical precipitator or filter baghouse) where the flue gas contains the combustion fly ash. In a spray-dryer system, the alkaline sorbent is usually lime slurry. The slurry is atomized and sprayed into a vessel as a cloud of fine bubbles where it contacts the hot flue gas. The water is completely evaporated by the hot gas and the residence time in the vessel (about 10 seconds) allows the SO2 and any other acid gases, such as SO3 and HCl, to react with the lime to form a dry powder of calcium sulfite, calcium sulfate and unreacted lime.
The dry powder is removed from the flue gas along with the combustion fly ash in the particulate removal equipment. Some of the solids from the particulate removal equipment (i.e., fly ash, calcium sulfite, calcium sulfate and unreacted lime) may be recycled and reused as part of the sorbent slurry.
Dry sorbent injection
The dry FGD system simply injects powdered lime or limestone sorbent directly into the flue gas. As shown in the adjacent location diagram, the dry sorbent may be injected into any one of three locations: (a) the upper section of the steam generator, (b) the economizer section of the steam generator or (c) the ducting between the air preheater and the electrostatic precipitator.
The powdered sorbent is pneumatically injected through lances designed to distribute the sorbent evenly across the flow path of the flue gas.
When injected into the upper section of the steam generator, it should enter at a point where the temperature range is about 900 to 1200 °C. Injection into the economizer should be at a point where the temperature range is about 400 to 600 °C. Injection into the ducting between the preheater and the precipitator should be at point where the flue gas temperature is about 150 to 180 °C.
The SO2 reacts directly with the powdered sorbent and the spent sorbent is removed from the flue gas along with the combustion fly ash in the particulate removal equipment.
Sulfur dioxide emission removal performance levels
Partial flue gas desulfurization can achieve about 50 to 70 percent removal of sulfur dioxide by the injection of dry limestone just downstream of the air preheater. The resultant solids are recovered in the electrostatic precipitators along with the fly ash.
In power plants burning pulverized coal, wet flue gas desulfurization that contacts the flue gases with lime slurries (in what are called wet lime scrubbers) can achieve 95% sulfur dioxide removal without additives and 99+% removal with additives. Wet FGD has the greatest share of the FGD usage in the United States and it is well established and commercially proven technology.
The typical older FGD units in power plants burning pulverized coal within the United States achieve average sulfur dioxide emission levels of about 0.340 kilograms of SO2 per megawatt hour (kg/MWh) which is equivalent to 0.22 pounds of SO2 per million British Thermal Units (lb/106 Btu) and which meets the level to which those units were permitted.
The lowest demonstrated sulfur dioxide emission level (in 2005) for power plants burning pulverized high-sulfur coal within the United States was 1.08 kg/MWh (0.07 lb SO2/106 Btu) and 0.046 kg/MWh (0.03 lb SO2/106 Btu) for plants burning low-sulfur pulverized coal.
Sulfuric acid mist formation
Fossil fuels such as coal and oil contain significant amounts of sulfur. When burned, about 95 percent or more of the sulfur is generally converted to sulfur dioxide. This happens under normal conditions of temperature and of oxygen present in the flue gas. However, there are circumstances under which this may not be the case.
For example, when the flue gas has too much oxygen and the sulfur dioxide is further oxidized to sulfur trioxide (SO3). Actually, too much oxygen is only one of the ways that SO3 is formed. Gas temperature is also an important factor. At about 800 °C, formation of SO3 is favored. Another way that SO3 can be formed is through catalysis by trace metals in the fuel. This is particularly true for heavy fuel oil, where small amounts of vanadium are present and which act as a catalyst.
In whatever way that SO3 is formed, it does not behave like SO2 in that it forms a liquid aerosol known as sulfuric acid (H2SO4) mist that is very difficult to remove. Generally, about 1% of the sulfur dioxide will be converted to sulfur trioxide. Since sulfur trioxide is an acid gas, just as is sulfur dioxide, it is also removed by the alkaline sorbents used in FGD systems.
Alternative methods of reducing sulfur dioxide emissions
An alternative to removing sulfur dioxide from the flue gases after combustion is to remove the sulfur from the fuel before or during combustion. Catalytic hydrodesulfurization has been used for treating petroleum fuel oils.
Fluidized bed combustion (FBC) adds lime to the fuel during combustion. The lime reacts with the SO2 in the flue gas to form sulfates which become part of the combustion ash and are removed in the particulate removal equipment.
Miscellaneous fact and statistics
The information in this section was obtained from a U.S. EPA published fact sheet dated 2003.
Flue gas desulfurization scrubbers have been applied to combustion units firing coal and oil that range in size from 5 MW to 1500 MW. Dry scrubbers and spray scrubbers have generally been applied to units smaller than 300 MW.
Approximately 85% of the flue gas desulfurization units installed in the US are wet scrubbers, 12% are spray dry systems and 3% are dry injection systems.
The highest SO2 removal efficiencies (greater than 95%) are achieved by wet scrubbers and the lowest (less than 80%) by dry scrubbers. However, the newer designs for dry scrubbers are capable of achieving efficiencies in the order of 90%.
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