DETAILED DESCRIPTION OF THE INVENTION

[0030] The present invention will now be described more in detail.

[0031] In the waste gas processing of the present invention for processing a waste gas containing sulfur oxides (SO _x ) and the metal mercury (Hg), the metal mercury is oxidized into mercury chloride in a catalytic oxidizing apparatus, followed by carrying out a wet desulfurization by using an alkaline absorption solution. In the present invention, the waste gas temperature in the inlet port of the catalytic oxidizing apparatus is measured, and a temperature control means using a heating means such as a heater or steam or a heat exchanger such as a gas-gas heater (GGH) is arranged on the upstream side of the catalytic oxidizing apparatus so as to control the waste gas temperature to fall within a prescribed temperature range. Also, the metal mercury concentration or the mercury chloride concentration in the waste gas is consecutively measured at the outlet port of the catalytic oxidizing apparatus so as to permit the temperature control means or the heat exchanger referred to above to control the waste gas temperature in the inlet port of the catalytic oxidizing apparatus based on the measured mercury concentration. As a result, it is possible to oxidize efficiently the metal mercury into mercury chloride under the most effective temperature.

[0032] FIG. 1 shows an example of the system (apparatus for removing mercury from a waste gas) in the case of using the methods described above. The specific embodiment of the processing method of the present invention will now be described in detail with reference to the drawing.

[0033] In the present invention, a waste gas containing SO _x and mercury is processed in the presence of a solid catalyst so as to oxidize the metal mercury into mercury chloride, followed by performing a wet desulfurization by using an alkaline absorbing solution. In carrying out the particular processing method, the waste gas is brought into contact with an absorbing solution such as a lime slurry circulating solution in a desulfurizing absorption tower arranged within the system so as to permit removal by absorption of SO _x . Also, among the mercury contained in the waste gas, mercury chloride (HgCl ₂ ) is dissolved in the absorbing solution so as to be removed. However, the solubility in water of the metal mercury among the mercury contained in the waste gas is very low and, thus, is not removed by the absorbing solution. As a result, the metal mercury is contained in the waste gas from the desulfurizing absorption tower in the form of a metal mercury vapor so as to pass through the desulfurizing absorption tower 7 .

[0034] Such being the situation, in the present invention, the metal mercury is converted into a water-soluble mercury chloride by a catalytic oxidizing apparatus arranged upstream of the desulfurizing apparatus and, then, the waste gas containing mercury chloride is guided into the desulfurizing absorption tower.

[0035] In the system shown in FIG. 1, a denitrification apparatus 2 , an air heater (A/H) 3 , a dust collector 4 , a heat exchanger 5 for recovering the heat energy, a catalytic oxidizing apparatus 6 , a desulfurizing absorption tower (wet desulfurizing apparatus) 7 , a re-heater 8 and a chimney 9 are arranged downstream of a boiler 1 in the order mentioned. The system also comprises a temperature control apparatus 10 to which are supplied signals denoting a gas temperature Y in the inlet port “a” of the catalytic oxidizing apparatus 6 and a Hg concentration at the outlet port “b” and a heating medium flow rate control valve 11 to which a flow rate control signal is supplied from the temperature control apparatus 10 .

[0036] The dust collector 4 included in the system shown in FIG. 1 is not particularly limited as far as it is possible to collect a coarse dust before the waste gas is introduced into the desulfurizing absorption tower 7 . Also, the desulfurizing absorption tower 7 is not particularly limited. For example, it is possible to use a wet desulfurizing apparatus generally used for the processing of a flue gas or a desulfurizing apparatus having a cooling tower arranged in the front stage of the absorption tower.

[0037] It the wet desulfurizing system of the construction described above, the re-heater 8 , etc. are arranged downstream of the desulfurizing absorption tower 7 , and the waste gas is released into the air atmosphere from the chimney 9 through these apparatuses. It should be noted that the combustion waste gas of a lowered temperature is heated in the re-heater 8 by the heat energy recovered by the heat exchanger 5 in the front stage of the desulfurizing absorption tower 7 . It should be noted in this connection that, if the waste gas of a lowered temperature is released as it is to the air atmosphere through the chimney 9 , a problem is generated that a white smoke caused by, for example, a water vapor is generated. Such being the situation, in releasing the combustion waste gas into the air atmosphere, a gas after the cleaning is heated so as to permit a high temperature gas to be released into the air atmosphere. Therefore, in the present invention, the re-heater 8 for supplying heat to the waste gas is arranged downstream of the wet desulfurizing apparatus 7 .

[0038] Incidentally, each of the heat exchanger 5 and the re-heater 8 is formed of a gas heater of the type that the heat energy is exchanged with a heating medium A used as a medium. It suffices for each of the heat exchanger 5 and the re-heater 8 to cool or heat the waste gas and, thus, it is possible for each of the heat exchanger 5 and the re-heater 8 to be a gas-gas heater for directly performing a heat exchange even if these heat exchanger 5 and re-heater 8 belong to different systems.

[0039] Chlorine contained in the fuel is present in the form of HCl in the waste gas generated from the boiler 1 , and the metal mercury (Hg) is oxidized into mercury chloride (HgCl ₂ ) in the presence of a catalyst within the catalytic oxidizing apparatus 6 . In the desulfurizing absorption tower 7 , SO ₂ contained in the waste gas is removed together with HgCl ₂ . The HCl concentration is markedly higher than the Hg concentration in the waste gas and, thus, an excessively large amount of HCl is contained in the waste gas. However, since HCl is absorbed by an alkaline aqueous solution such as a lime water in the desulfurizing apparatus, HCl is not released into the air atmosphere through the chimney. The waste gas having Hg removed in the desulfurizing absorption tower 7 is introduced into the re-heater 8 so as to be heated by the heat energy recovered by the heat exchanger 5 and, then, is released into the air atmosphere through the chimney 9 .

[0040] In the present invention of the particular construction described above, the metal mercury is oxidized into a water-soluble mercury compound in the presence of a solid catalyst, and the water-soluble mercury compound within the waste gas is removed in the wet desulfurizing process step. It should be noted in this connection that the optimum temperature for applying an oxidizing treatment to the metal mercury is changed depending on the Cl content in the fuel. Therefore, a problem is generated that the metal mercury is not sufficiently oxidized because the waste gas temperature is excessively higher or lower than the optimum temperature noted above so as to cause the metal mercury to be discharged into the air atmosphere.

[0041] Under the circumstances, in the embodiment of the present invention, the gas temperature within the catalytic oxidizing apparatus 6 is controlled to an appropriate temperature by adjusting the flow rate of the heating medium A supplied into the heat exchanger 5 arranged on the upstream side depending on the gas temperature in the inlet port “a” of the catalytic oxidizing apparatus 6 and/or the metal mercury concentration or the mercury chloride concentration in the outlet port “b”.

[0042] Where the gas temperature within the catalytic oxidizing apparatus 6 is controlled by detecting the gas temperature at the inlet port “a” of the catalytic oxidizing apparatus 6 , the gas temperature Y at the inlet port “a” of the catalytic oxidizing apparatus 6 is detected and compared with a reference temperature set in advance within the temperature control apparatus 10 depending on the kind of the fuel, and a flow rate control signal Z determined from the amount of change is supplied into the heating medium flow rate control valve 11 . The amount of the heating medium supplied into the heat exchanger 5 is changed by adjusting the heating medium flow rate control valve 11 so as to control the gas temperature in the outlet port of the heat exchanger 5 at an appropriate temperature.

[0043] As described above, the apparatus for removing mercury from a waste gas, which is shown in FIG. 1 , comprises the catalytic oxidizing apparatus 6 , in which the metal mercury contained in the combustion waste gas containing SO _x and mercury is oxidized into mercury chloride in the presence of a solid catalyst and under the reaction temperature not higher than 300° C., the desulfurizing absorption tower 7 in which mercury is removed by an alkaline absorbing solution, and the temperature control apparatus 10 for controlling the reaction temperature in oxidizing the metal mercury into mercury chloride. The particular construction of the present invention makes it possible to control the gas temperature in the outlet port of the heat exchanger 5 at an appropriate temperature. It follows that the metal mercury can be oxidized stably into mercury chloride even if a chlorinating agent such as HCl is not added to the reaction system so as to remove effectively the metal mercury from the waste gas.

[0044] The following description covers the case where the gas temperature in the catalytic oxidizing apparatus 6 is controlled by detecting the mercury concentration in the outlet port “b” of the catalytic oxidizing apparatus 6 .

[0045] It should be noted that the metal mercury concentration in the inlet port “a” of the catalytic oxidizing apparatus 6 is determined by the kind of the fuel. On the other hand, the metal mercury concentration or the mercury chloride concentration in the outlet port “b” of the catalytic oxidizing apparatus 6 is determined by the relationship among the oxidizing rate of the metal mercury, the Hg concentration in the inlet port of the catalytic oxidizing apparatus 6 , and the Hg concentration in the outlet port of the catalytic oxidizing apparatus 6 , as shown in formulas (2) and (3) given below:

C _out =C _in (1−η) (2)

C′ _out =C _in ·η (3)

[0046] where C _in represents the Hg concentration in the inlet port of the catalytic oxidizing apparatus 6 , C _out represents the Hg concentration in the outlet port of the catalytic oxidizing apparatus 6 , C′ _out represents the HgCl ₂ concentration in the outlet port of the catalytic oxidizing apparatus 6 , and η represents the oxidizing rate of the metal mercury.

[0047] As apparent from formulas (2) and (3) given above, the appropriate temperature can be obtained from the relationship between the catalyst temperature and the oxidizing rate of the metal mercury.

[0048] Under the circumstances, in the embodiment of the present invention, the gas temperature Y in the inlet port “a” of the catalytic oxidizing apparatus 6 and the concentration X of the metal mercury or mercury chloride in the outlet port “b” of the catalytic oxidizing apparatus 6 are detected, and the signal denoting the detected values are supplied to the temperature control device 10 . In the temperature control device 10 , the mercury oxidizing rate is calculated on the basis of the concentration X of the metal mercury or mercury chloride, and the optimum temperature is calculated from the relationship between the catalyst temperature set in advance depending on the kind of the fuel and the oxidizing rate of the metal mercury. Also, the gas temperature within the catalytic oxidizing apparatus 6 is compared with the gas temperature Y referred to above, and a flow rate control signal Z obtained from the amount of the change is supplied into the heating medium flow rate control valve 11 . The amount of the heating medium supplied into the heat exchanger 5 is changed by the adjustment of the heating medium flow rate control valve 11 so as to control the gas temperature in the outlet port of the heat exchanger 5 at an appropriate temperature.

[0049] The waste gas processed in the present invention includes, for example, a waste gas generated from a thermoelectric power station utilizing combustion of a fuel containing sulfur and mercury such as coal or a heavy hydrocarbon oil, a waste gas generated from a boiler used in, for example, a factory, and a waste gas generated from a heating furnace included in a metal factory, a petroleum refinery, a petrochemical plant, etc. What should be noted is that the a large amount of a waste gas containing carbon dioxide, oxygen, SO _x , smuts or water is processed by the method and apparatus of the present invention.

[0050] The conventional wet desulfurizing apparatus can be used in the present invention. The absorbing solution used for the wet desulfurization includes an aqueous solution (alkaline absorbing solution) of absorbents such as calcium carbonate, calcium oxide, calcium hydroxide, sodium carbonate and caustic soda.

[0051] The solid catalyst used in the present invention includes a catalyst prepared by allowing at least one active species selected from the group consisting of Pt, Ru, Rh, Rd, Ir, V, W, Mo, Ni, Co, Fe, Cr, Cu and Mn to be supported by at least one carrier selected from the group consisting of TiO ₂ , SiO ₂ , ZrO ₂ , Al ₂ O ₃ and WO ₃ and/or zeolite. Also, it is possible to use a solid catalyst prepared by allowing at least one kind of a VIII group metal selected from the group consisting of nickel (Ni), ruthenium (Ru), rhodium (Rh), palladium (Pd) and platinum (Pt), silver sulfate or a precursor material of silver sulfate to be contained in a carrier such as a hydroxide or an oxide of at least one kind of a IV group metal selected from the group consisting of silicon (Si), titanium (Ti), and zirconium and/or hydroxide or oxide of aluminum, followed by calcining the resultant structure so as to stabilize the resultant structure.

[0052] It is particularly desirable to use titanium as a carrier. It should be noted that a catalyst prepared by allowing at least one kind of an oxide selected from the group consisting of an oxide of vanadium, tungsten or molybdenum to be supported as an active metal species in a carrier formed of a composite oxide of titanium exhibits a satisfactory activity.

[0053] In the present invention, it is desirable to use a titanium oxide in the form of a composite oxide in order to increase the specific surface area and the amount of the solid acid of the decomposing catalyst. The metal forming the composite oxide together with titanium includes, for example, silicon (Si), zirconium (Zr), aluminum (Al) and tungsten (W). To be more specific, it is possible to use a composite oxide containing titanium and silicon, a composite oxide containing titanium and zirconium, a composite oxide containing titanium and aluminum, and a composite oxide containing titanium and tungsten. Any of these composite oxides is unlikely to form a sulfate and, thus, permits maintaining a stable structure so as to make it possible to increase the specific surface area and the amount of the solid acid.

[0054] It is also possible to use a ternary composite oxide such as a composite oxide containing silicon and zirconium together with titanium, a composite oxide containing silicon and tungsten together with titanium, a composite oxide containing silicon and aluminum together with titanium, a composite oxide containing zirconium and aluminum together with titanium, and a composite oxide containing zirconium and tungsten together with titanium.

[0055] The composition of the carrier in the case of a composite oxide is not particularly limited. However, it is desirable for the carrier to contain, for example, 70 to 95 parts by weight of titanium and 30 to 5 parts by weight of an oxide of silicon (Si), zirconium (Zr), aluminum (Al) and/or tungsten (W). If the amount of the oxide falls within the range noted above, the catalyst contains the largest amount of the solid acid so as to exhibit a high catalytic activity. If the amount of the oxide fails to fall within the range noted above, it is impossible to obtain a sufficiently large amount of the solid catalyst.

[0056] Any metal salt such as a chloride, a sulfate and a nitrate can be used as the raw material for providing the elements forming the composite oxide. To be more specific, the metal salt in the form of an aqueous solution is dripped into an alkali aqueous solution such as an aqueous solution of ammonia or sodium carbonate so as to achieve co-precipitation. It is also possible to use each metal alkoxide raw material so as to obtain a complex hydroxide by means of, for example, hydrolysis. The complex hydroxide cake formed by the co-precipitation or hydrolysis is washed and, then, dried, followed by baking the dried cake under temperatures falling within a range of between 200° C. and 650° C. so as to obtain a desired composite oxide. It should be noted that, if the baking temperature is lower than 200° C., it is impossible to retain the metal salt in the form of an oxide. On the other hand, if the baking temperature exceeds 650° C., the particles are fused to each other so as to decrease the surface area of the catalyst.

[0057] In the catalyst used in the present invention, at least one element selected from the group consisting of Pt, Ru, Rh, Pd, Ir, V, W, Mo, Ni, Co, Fe, Cr, Cu and Mn is supported on the composite oxide used as a carrier. Any of the oxides exemplified above exhibits an oxidizing power so as to make it possible to oxidize th metal mercury into mercury chloride. Also, any of the oxides referred to above is excellent in durability relative to a sulfur compound and a heavy metal.

[0058] The components and the mixing ratio of the components of the catalyst composition are not particularly limited in the present invention. However, in a typical example, it is desirable for the catalyst to comprise 1 to 20 parts by weight of the catalytic component in the case of a one component system such as vanadium pentoxide relative to 100 parts by weight of the carrier consisting of a single kind of an oxide or a composite oxide. Likewise, in the case of a binary system, it is desirable to use a catalyst containing 1 to 10 parts by weight of vanadium pentoxide and 2 to 25 parts by weight of tungsten trioxide or a catalyst containing 1 to 10 parts by weight of vanadium pentoxide and 2 to 25 parts by weight of molybdenum trioxide. Likewise, in the case of a ternary system, it is desirable to use a catalyst containing 1 to 10 parts by weight of vanadium pentoxide, 1 to 20 parts by weight of tungsten trioxide and 1 to 20 parts by weight of molybdenum trioxide.

[0059] The catalytic activity of the catalyst is increased with increase in the amount of the active metal supported by the carrier. However, if the active metal is excessively supported by the carrier, it is possible to promote a side reaction such as the reaction to convert SO ₂ into SO ₃ . Such being the situation, it is desirable for the amount of the active metal to fall within the range noted above. Incidentally, SO ₃ generates a problem that corrosion of the equipment is brought about. Also, it is possible to use the metal oxide noted above singly. Alternatively, it is also possible to add an inorganic material to the metal oxide or to have the metal oxide supported by a substrate for use in the present invention.

[0060] Also, in the present invention, it is possible to use a solid catalyst prepared by allowing at least one kind of a VIII group metal selected from the group consisting of nickel, ruthenium, rhodium, palladium and platinum and a sulfate group or a precursor material of the sulfate group to be supported by a carrier consisting of a hydroxide or an oxide of at least one IV group metal selected from the group consisting of silicon, titanium and zirconium and/or a hydroxide or an oxide of aluminum, followed by baking the resultant structure so as to stabilize the resultant structure.

[0061] It is possible for the catalyst used in the catalytic oxidizing apparatus to be integrally molded and to assume an optional shape. For example, it is possible for the catalyst noted above to have a shape of a pellet, a plate or a cylinder. It is also possible for the catalyst to be corrugated or to have a honeycomb structure. Incidentally, it is naturally desirable for the catalyst to have a large contact area with the gas. However, it is undesirable for the catalyst to have an excessively large contact area with the gas because the fluidizing back pressure of the waste gas is increased depending on the degree of the loading density of a powdery catalyst. As a measure against the difficulty, it is desirable in general to use a molded catalyst of, for example, a honeycomb structure obtained by compressing a powdery catalyst to have a prescribed density without excessively decreasing the specific surface area of the catalyst.

[0062] In order to confirm the effect of removing mercury produced by the present invention, experiments were conducted as follows. Needless to say, the present invention is not limited at all by the description of the examples described below.

[0063] Methods of preparing honeycomb catalysts 1 to 5 will now be described.

[0064] [Preparation of Honeycomb Catalysts 1 and 2]

[0065] In the first step, an aqueous solution of titanyl sulfate (TiSO ₄ ) and an aqueous solution of colloidal silica (Si ₂ ) were mixed with each other in the mixing ratio TiSO ₄ :SiO ₂ of 90:10 by weight, followed by heating the mixed aqueous solution to 70° C. Then, an aqueous solution of ammonia was dripped into the heated mixed aqueous solution until the mixed solution was allowed to exhibit a pH value of 7 so as to form a co-precipitated slurry. Further, the slurry was stirred and aged for 2 hours at 70° C., followed by filtering the aged slurry and washing the filtrate so as to obtain a cake-like material. The cake-like material thus obtained was dried at 100° C. and, then, baked at 500° C. for 5 hours so as to obtain a composite oxide of TiO ₂ ·SiO ₂ . The composite oxide thus obtained is called composite oxide 1 herein later.

[0066] In the next step, ammonium metavanadate was dissolved in an aqueous solution of methyl amine such that 5 parts by weight of V ₂ O ₅ is contained in the aqueous solution relative to 100 parts by weight of the composite oxide 1, and the resultant aqueous solution was dripped onto the powdery oxide noted above. The resultant mixture was repeatedly kneaded and dried so as to permit V ₂ O ₅ to be supported by the composite oxide, thereby obtaining a sample. The sample thus obtained was baked at 500° C. for 5 hours so as to obtain a powdery catalyst 1.

[0067] On the other hand, ammonium paratungstate and ammonium metavanadate were dissolved in an aqueous solution of methyl amine such that 8 parts by weight of WO ₃ and 5 parts by weight of V ₂ O ₅ were contained in the resultant solution relative to 100 parts by weight the composite oxide 1. Then, the resultant solution was dripped on the powdery composite oxide and the resultant mixture was repeatedly kneaded and dried so as to permit WO ₃ and V ₂ O ₅ to be supported by the composite oxide, thereby obtaining a sample. The sample thus obtained was baked at 500° C. for 5 hours so as to obtain a powdery catalyst 2.

[0068] Further, an ammonia water was added to a mixture including 3 parts by weight of a glass fiber used as a binder, 3 parts by weight of kaolin and 3 parts by weight of cellulose acetate used as an organic plasticizer, followed by kneading the mixture. The kneaded mixture was subjected to an extrusion molding so as to obtain an integral molding of a honeycomb structure having a pitch of 5.0 mm (wall thickness of 1.0 mm). The molding thus obtained was dried and, then, baked at 500° C. for 5 hours so as to remove the organic plasticizer, thereby obtaining honeycomb catalysts 1 and 2.

[0069] [Preparation of Honeycomb Catalyst 3]

[0070] A composite oxide 2 was obtained by a method similar to that employed for obtaining the composite oxide 1, except that zirconium oxynitride was added in place of the colloidal silica at a mixing ratio TiO ₂ :ZrO ₂ of 90:1 in the method of preparing the honeycomb catalysts 1 and 2. Then, a powdery catalyst 3 was obtained by using the composite oxide 2 by a method similar to that employed for obtaining the honeycomb catalysts 1 and 2. Further, a honeycomb catalyst 3 was prepared by a method similar to that employed for preparing the honeycomb catalysts 1 and 2.

[0071] [Preparation of Honeycomb Catalyst 4]

[0072] A zirconium hydroxide (Zr(OH) ₄ ) powder was impregnated with an aqueous solution of nickel sulfate containing 5 parts by weight of the metal nickel relative to 100 parts by weight of the carrier, followed by baking the impregnated zirconium hydroxide powder at 600° C. for 3 hours so as to obtain a powdery catalyst 4. Then, a honeycomb catalyst 4 was prepared by a method similar to that employed for preparing the honeycomb catalysts 1 and 2.

[0073] [Preparation of Honeycomb Catalyst 5]

[0074] A titanium oxide (TiO ₂ ) powder was impregnated with an aqueous solution of platinic chloride containing 0.5 part by weight of Pt relative to 100 parts by weight of the carrier, followed by baking the impregnated titanium oxide powder at 500° C. for 3 hours and subsequently reducing the baked material with hydrogen at 300° C. for 1 hour so as to obtain a powdery catalyst 5. Then, a honeycomb catalyst 5 was prepared by a method similar to that employed for preparing the honeycomb catalyst 1.

[0075] Some Examples of the present invention will now be described.

EXAMPLE 1

[0076] A test for evaluating the oxidizing rate of mercury and the mercury removal rate in an absorbing bottle was conducted in respect of each of three kinds of catalysts by using an apparatus for removing mercury from a waste gas shown in FIG. 2 . In the apparatus used in Example 1, a CO ₂ gas, an O ₂ gas, a H ₂ O vapor and HCl were added to a N ₂ gas, and the mixed gas thus prepared was mixed with a vapor of the metal mercury so as to prepare a pseudo gas 11 .

[0077] The pseudo gas 11 thus prepared was introduced into a reactor 12 provided with a catalytic oxidizing apparatus 6 , and the catalyst temperature was controlled by an electric heater 13 . The gas at the outlet port of the catalytic oxidizing apparatus 6 was partly introduced into an absorbing bottle 14 .

[0078] The test was conducted under a gas amount of 90 l (liters) N/h(w), a catalyst SV of 3000 h ⁻ , a catalyst temperature of 120° C., a mercury concentration of 20 μg/m ³ N, and a HCl concentration of 1 ppm, as shown in Table 1. The other test conditions are also shown in Table 1. 1

[0079] During the test, an inlet gas “a” and an outlet gas “b” of the catalyst were sampled so as to measure the mercury concentration. The mercury chloride concentration was measured in the outlet gas “b” so as to obtain the mercury oxidizing rate with the catalyst by formula (4) given below:

L=M/N× 100 (4)

[0080] where L represents the mercury oxidizing rate (%), M represents the HgCl ₂ concentration at the catalyst outlet port, and N represents the Hg concentration at the catalyst inlet port.

[0081] A gas c at the outlet port of the absorbing bottle was also sampled so as to measure the mercury removal rate in the absorbing bottle by formula (5) given below:

U= ( V−M )/ V× 100 (5)

[0082] where U represents the mercury removal rate (%), V represents the Hg concentration at the catalyst inlet port, and M represents the Hg concentration at the outlet port of the absorbing bottle.

[0083] The mercury oxidizing rates of the honeycomb catalysts 1, 2 and 3 were found to be 90%, 94% and 92%, respectively, supporting that each of these honeycomb catalysts exhibits a high mercury oxidizing rate. Also, the mercury removal rates in the absorbing bottle 14 were found to be 92%, 95% and 94% in the cases of using the honeycomb catalysts 1, 2 and 3, respectively, so as to support a high mercury removing performance. In conclusion, it has been clarified that the mercury removal system is effective even under a relatively low temperature and a low HCl concentration.

EXAMPLE 2

[0084] A test for evaluating the oxidizing rate of mercury and the mercury removal rate in an absorbing bottle was conducted as in Example 1 in respect of two additional catalysts (honeycomb catalysts 4 and 5) by using the apparatus shown in FIG. 2 under a further lower temperature of 90° C. The test conditions for Example 2 were as shown in Table 2 given below: 2

[0085] The mercury removal rates in the cases of using the honeycomb catalysts 4 and 5 were found to be 88% and 85%, respectively, supporting a high mercury oxidizing performance achieved in the cases of using each of these honeycomb catalysts 4 and 5. On the other hand, the mercury removal rates in the absorbing bottle in the cases of using the honeycomb catalysts 4 and 5 were found to be 90% and 88%, respectively, supporting a sufficiently high mercury removing performance.

EXAMPLE 3

[0086] A test for evaluating the oxidizing rate of mercury and the mercury removal rate in a desulfurizing absorption tower was conducted by using an apparatus for removing mercury from a waste gas shown in FIG. 4 in respect of three kinds of catalysts. Table 3 given below shows the test conditions. 3

[0087] The gist portions of the apparatus shown in FIG. 4 will now be described. Some members of the apparatus shown in FIG. 4 are equal to those of the apparatus shown in FIG. 1 , and the common members are denoted by the same reference numerals so as to avoid the overlapping description.

[0088] A reference numeral 21 shown in FIG. 4 denotes a combustion furnace into which an air stream A and a finely pulverized coal B are continuously supplied for the combustion of the coal B so as to generate a combustion waste gas. An air pre-heater 22 , an electric dust collector 23 , a cooler 24 , a catalytic oxidizing apparatus 6 , a desulfurizing absorption tower 7 , a heat exchanger 26 and a chimney 9 are connected in the order mentioned to the combustion furnace 21 . Electric heaters 27 for controlling the waste gas temperature are arranged on the upper and lower sides of the catalytic oxidizing apparatus 6 . Further, a cooling water is supplied into the cooler 24 through a pipe 29 having a flow rate adjusting valve 28 mounted thereto.

[0089] An air stream A and the finely pulverized coal B were continuously supplied into the combustion furnace 21 for the combustion of the coal B so as to generate a combustion waste gas. Also, a mercury vapor C was added to the combustion waste gas upstream of the air pre-heater 22 because the mercury concentration in the combustion waste gas was low, i.e., several μg/m ³ N, so as to increase the mercury concentration in the inlet port of the air pre-heater 22 to about 10 μg/m ³ N. The combustion waste gas was supplied as a gas having a temperature of about 120° C. to the catalytic oxidizing tower 6 through the air pre-heater 22 , the electric dust collector 23 , and the cooler 24 supplied with a cooling water E. Incidentally, the electric heater 27 was controlled at 120° C. so as to prevent the temperature of the waste gas from being lowered by, for example, the heat dissipation. The waste gas passing through the catalyst bed was supplied to the desulfurizing absorption tower 7 through which was circulated a slurry of an absorbing solution having a lime D added thereto so as to remove SO ₂ and HgCl ₂ contained in the waste gas. Further, the waste gas cleansed in the desulfurizing absorption tower 7 was discharged to the outside from the chimney 9 through the heat exchanger 26 .

[0090] During the operation described above, the mercury concentration was measured at the inlet port “a” and the outlet port “b” of the catalytic oxidizing apparatus 6 . The mercury chloride concentration was also measured at the outlet port “b” of the catalytic oxidizing apparatus 6 so as to obtain the mercury oxidizing rate achieved by the catalyst. Further, the mercury concentration was measured at the outlet port “c” of the desulfurizing absorption tower 7 so as to obtain the rate of mercury removal achieved in the desulfurizing absorption tower 7 .

[0091] The mercury oxidizing rates achieved by the honeycomb catalysts 1, 2 and 3 were found to be 92%, 95% and 94%, respectively, supporting a high mercury oxidizing performance of each of these honeycomb catalysts. Also, the mercury removal rates in the absorbing bottle were found to be high, i.e., 94%, 96% and 95% in the cases of using the honeycomb catalysts 1, 2 and 3, respectively. In conclusion, it has been clarified that the present invention also provides an effective mercury removing system in the processing of a combustion waste gas.

EXAMPLE 4

[0092] The stability of the mercury oxidizing performance was evaluated by using the mercury removing apparatus shown in FIG. 4 and the honeycomb catalyst 1. The mercury removing apparatus was operated under the conditions equal to those for Example 3. Specifically, the waste gas temperature X at the inlet port “a” of the catalytic oxidizing apparatus 6 was detected, and a flow rate adjusting signal Z was supplied to the flow rate adjusting valve 28 of the cooling water E based on the difference between the waste gas temperature X noted above and a reference temperature supplied to the temperature control apparatus 10 so as to control the gas temperature at the inlet port of the catalytic oxidizing apparatus 6 by adjusting the flow rate of the cooling water E. As a result, it has been confirmed that it is possible to control the oxidizing rate of mercury to fall within a range of 92±1% by controlling the gas temperature at 120±5° C.

[0093] Also, the gas temperature in the inlet port of the catalytic oxidizing apparatus 6 was controlled similarly by detecting the metal mercury concentration Y in the outlet port “b” of the catalytic oxidizing apparatus 6 . As a result, it has been confirmed that it is possible to control the oxidizing rate of mercury to fall within a range of 92±1% by controlling the gas temperature at 120±5° C.

[0094] As described above, it has been clarified that a stable mercury oxidizing performance can be maintained by controlling the catalyst temperature.