PROCESS, APPARATUS AND SYSTEM FOR THE TREATMENT OF FLUE GAS

Abstract: A processor for an exhaust gas in which finely powdered solid pollutants and gaseous atmosphere pollutants exist in mixture, wherein a gas suction port (29a) for sucking an exhaust gas is formed in a funnel (27) tapered downward, jet nozzles (30a, 30b, 30c) for jetting a compressed gas along the inner wall of the funnel (27) are disposed in the proximity of the gas suction port (29a) and an exhaust port (27a) is formed at a lower part of the funnel (27).

Description: Technical Field The present invention relates to a flue gas treatment apparatus, a flue gas treatment system, both of which are suitable for use in the treatment of flue gas in which a fine solid particulate contaminant and a gaseous air pollutant are mixed, and a process for treating a flue gas. Background Art In flue gas, substances present in a solid form, such as dust, are generally mixed with additional air pollutants present in a gaseous form, for example, NOx. Known conventional removal means for fine solid particles in flue gas include cyclones making use of centrifugal force and bag filters relying upon filtration. They are all employed to separate and collect only fine solid particles from flue gas. They cannot eliminate gaseous air pollutants so most of such air pollutants are released into the atmosphere. To remove such gaseous air pollutants, a chemical facility is additionally required using an aqueous solution which can absorb such air pollutants. In addition to a reaction tank in which the gaseous air pollutants react with the aqueous solution, this chemical facility is also equipped with an apparatus for recirculating the aqueous solution within the facility, an apparatus for feeding a fresh aqueous solution, an apparatus for treating the aqueous solution, etc. To treat flue gas which contains a contaminant present in a solid form and an air pollutant in a gaseous form, a system constructed with a combination of a dust collector, such as a cyclone, and a chemical facility has heretofore generally been employed. Such a conventional flue gas treatment system is, however, accompanied by the drawback that a very large chemical facility is required. Furthermore, the need to take into consideration the corrosion resistance to the aqueous solution leads to higher initial costs for the system, and the need for supply and treatment of the aqueous solution results in higher running costs. In industrial fields where flue gas occurs in a huge volume during the course of manufacture of a product or the like, such as in the chemical and steel industries, there has hence been a strong desire for the development of a flue gas treatment system which can eliminate gaseous air pollutants without any chemical facility. For industrial fields in which an apparatus such as a small incinerator or boiler is used, such a flue gas treatment system is too large and too expensive. It is the current situation that, despite the immense concern about the pollution problem, no flue gas treatment system or apparatus is installed. Disclosure of the Invention The present invention has been developed with the foregoing conventional problems in mind. It is an object of the present invention to provide an apparatus, a system and a method for the treatment of flue gas, which do not require any chemical facility and thus high initial and running costs. To achieve the above object, this invention provides a flue gas treatment apparatus which comprises: a closed funnel (which may also be described as a conical cylinder) with an upper shroud, an inlet portion for drawing flue gas provided in the upper part of the funnel, one or several jet nozzles for jetting out a compressed gas, preferably air, along the upper inner peripheral wall of the funnel, and a discharge port provided in the lower part of the funnel. According to a preferred embodiment the present invention provides a flue gas treatment apparatus which is characterized in that an outer cyclinder is provided enclosing at least the upper part of the funnel, and that the inlet portion is a clearance which is formed between the upper-end peripheral edge of the funnel and the lower-end peripheral edge of the shroud. The clearance guides the flue gas, which has flowed into the outer cylinder into the inner funnel. In the apparatus for treating flue gas a gas suction port may be provided between the inner wall of the outer cylinder and the outer wall of the funnel in its lower part. Another preferred apparatus according to the present invention is characterized by one or more of the following features: an odd number of jet nozzles are provided, the jet nozzles are arranged at equal angular intervals on the circular periphery of a shroud, the jet nozzles are arranged such that the jetting direction is tangential relative to the inner peripheral wall of the funnel and the jetting angle of each of the jet nozzles is set such that the outermost boundary of the jetted air substantially reaches the adjacent jet nozzle. To achieve the above object, this invention also provides a flue gas treatment system comprising the above-described flue gas treatment apparatuses, the inlet portion of which is connected to a flue gas source, and a source for compressed gas for feeding the compressed gas to the jet nozzle or nozzles. A plurality of such flue gas treatment apparatuses can be provided in series and/or parallel with the flue gas source. Further, a cyclone dust collector can be arranged on the upstream and/or downstream side of the flue gas treatment apparatus. The present invention also provides a process for the treatment of flue gases containing fine solid particles; this process is characterized in that the flue gas is introduced into the upper part of a funnel with an upper shroud together with a compressed, jetted out gas, preferably air, along the upper inner peripheral wall of the funnel, forming an eddy current, such that the pressure rises as a result of the introduction of the compressed air, and the temperature is decreased because of adiabatic expansion of the compressed gas, and liquid water is formed, which is discharged from the lower part of the funnel together with fine solid particles. This process is carried out with one of the above mentioned apparatuses or with a system according to the present invention. As a result of several tests and extensive study, the inventors have found that, as described above, gaseous and fine solid particulate contaminants or pollutants in flue gas can be removed by a relatively simple system without the need for the provision of any chemical facility although some of its detailed mechanism has not been fully elucidated until now. To describe the system briefly, a compressed gas is jetted against a conical inner cylinder, an eddy current is formed by the compressed gas inside the inner cylinder, and solid contaminants are then removed by the resultant centrifugal force. At the same time, the temperature inside the inner cylinder is lowered by a pressure increase inside the inner cylinder by the supply of the compressed gas, adiabatic expansion of the compressed gas, and the like, so that gaseous contaminants are liquefied. The resulting liquefied contaminants are then adsorbed on the solid contaminants so that the liquefied contaminants are removed. Before describing the present invention in detail, a principle due to which this invention can bring about the aforementioned advantages will be described taking nitrogen oxides as an example for the sake of convenience. Among pollutants responsible for air pollution, nitrogen oxides are considered to be the most serious pollutants these days. Of these, nitrogen dioxide NO 2 is the gas which has caused particular concern in recent years with respect to the induction of the photochemical "smog" phenomenon and also for the release of its distinct offensive odor. Nitrogen oxides occur during the combustion of fossil fuels such as coal or petroleum or in a chemical process for the production of nitric acid and the like. Among these nitrogen oxides, nitrogen monoxide NO is formed as a result of a direct reaction of oxygen with nitrogen upon combustion of the above-mentioned fossil fuels whereas nitrogen dioxide NO 2 is formed when nitrogen monoxide is subjected to further oxidation. When cooled, this NO 2 undergoes a bimolecular bonding reaction and changes into colorless liquid nitrogen tetraoxide (N 2 O 4 ). This reaction may be expressed as follows: 2NO 2 ↔ N 2 O 4 + Q This reaction is a reversible reaction and an exothermic reaction. When the temperature drops, the equilibrium reaction (1) proceeds rightwards and, at 17°C under atmospheric pressure, the proportion of existing NO 2 drops to "0" and nitrogen dioxide changes completely to liquid nitrogen tetraoxide N 2 O 4 . The equilibrium reaction (1) also proceeds rightwards when the pressure increases. It is therefore possible to reduce the proportion of existing NO 2 to "0" by raising the pressure even when the temperature is higher than 17°C. Details of the above reaction are described in the Volume "Air" of the "Pollutant Analysis Guideline" published by the Kanto Branch of the Analytical Chemical Society of Japan. If fine particles are present in an atmosphere in which NO 2 has completely changed to liquid N 2 O 4 as described above, N 2 O 4 even in a trace amount is adsorbed on the fine particles and is thus removed. This principle will be described by applying it to the flue gas treatment apparatus according to the present invention. Flue gas from a flue gas source flows into the outer cylinder through the gas suction port of the outer cylinder. When the flue gas flows into the cylinder through the clearance between the outer cylinder and the inner funnel, the flue gas forms a rapid eddy current owing to the compressed gas jetted out through the jet nozzles. Inside the inner funnel, the pressure rises as a result of the entrance of the compressed gas but the temperature drops because of the adiabatic expansion of the compressed gas. Gaseous contaminants in the flue gas are liquefied due to the rise of pressure and the drop in temperature as described above. The air pollutants so liquefied collide with fine solid particulate contaminants in the rapid eddy current, whereby the former are adsorbed on the latter. These fine solid particles are removed under the action of centrifugal force. The air pollutants are therefore eliminated in the form adsorbed on the fine solid particles from the flue gas together with fine solid particles and are discharged through the discharge port. To enable the present invention to bring about advantages such as those described above, it is however necessary to appropriately design the number of jet nozzles, their arrangement, the jetting angle of the compressed gas, the shape of the conical inner cylinder, the shape and size of the clearance to allow flue gas to flow into the funnel, the flow rate of the flue gas, etc. Unless they are appropriate, the above-described advantages cannot be brought about fully. The present inventors were able to find out correlations among these parameters as a result of repetitive tests which were conducted over a long time. As a result of several incineration tests of industrial waste such as various synthetic resins and automobile tires, the present inventors have also found that the flue gas treatment apparatus according to the present invention also has deodorizing function. As far as is already confirmed to date, this deodorizing function is known to result from the removal of gaseous air pollutants and also the deodorizing action of unburnt carbon components contained in fine solid particles. The deodorizing action of these unburnt carbon components is considerably different from that of ordinary carbon because the environment and the like are different from the environment for the deodorization by ordinary carbon. This is attributed to the fact that unburnt carbon has a very large surface area because of its very fine particulate form and the deodorizing environment is under elevated pressure. Namely, the surface area of unburnt carbon is large and the pressure of the environment is high. This increases the probability of contact between unburnt carbon and odor molecules, whereby deodorizing reactions are allowed to proceed promptly. The present invention can also improve the collection efficiency for fine solid particles over that available from the use of an ordinary cyclone. When flue gas enters the funnel (conical cylinder), water vapor in the flue gas is liquefied due to a temperature drop so that water is formed. In addition, water is also formed upon production of compressed air. Fine solid particles are adsorbed on these water molecules, thereby making it possible to collect even those particles having substantially a small size. Brief Description of the Drawings FIGURE 1 to FIGURE 5 show a first embodiment of the present invention, in which FIGURE 1 is a fragmentary cross-section of a flue gas treatment system, FIGURE 2 is a transverse cross-section of a flue gas treatment apparatus, FIGURE 3 is a vertical cross-section of the flue gas treatment apparatus, FIGURE 4 is a flow sheet of the flue gas treatment system, and FIGURE 5 is a perspective view of the flue gas treatment system; and FIGURES 6 and 7 illustrate a second embodiment, in which FIGURE 6 is a flow sheet of another flue gas treatment system and FIGURE 7 is a table showing measurement results after the treatment of a flue gas. The embodiments of the present invention will hereinafter be described with reference to FIGURE 1 to FIGURE 7. A first embodiment of the present invention will now be described with reference to FIGURE 1 to FIGURE 5. The flue gas treatment system is constructed, as shown in FIGURE 4, of a cooler 2 connected to a flue-gas-producing boiler 1 to cool flue gas; blowers 3,11 for feeding flue gas into cyclones, etc.; cyclones 4a,4b for removing fine solid particles from flue gas fed by the blower 3; first auxiliary cyclones 5a,5b, second auxiliary cyclones 7a,7b, third auxiliary cyclones 8a,8b, fourth auxiliary cyclone 9, fifth auxiliary cyclone 10, sixth auxiliary cyclone 13 and seventh auxiliary cyclone 14, all of which serve to remove fine solid particles not removed by the upstream-side cyclones and the like; a multi-cyclone 12 for removing fine solid particles from flue gas fed by the blower 11; flue gas treatment apparatuses 15a,15b for removing gaseous and fine solid particulate contaminants from the flue gas; a compressor 21 for feeding compressed air to the flue gas treatment apparatuses 15a,15b; and a force feed screw 17 for conveying fine solid particles, which have been discharged from the cyclones, to a desired location. As is illustrated in FIGURE 1, the flue gas treatment apparatuses 15a,15b are each equipped with an inner funnel 27, an outer cylinder 28 enclosing the inner funnel 27, three jet nozzles 30a,30b,30c for jetting out compressed air along the upper inner peripheral wall of the inner funnel 27, a pressure gauge 24 and a shut-off valve 25. Formed in the lower part of the inner funnel 27 is a discharge port 27a through which fine solid particles and the like are discharged. In the lower part of the outer cylinder 28, a gas suction port 28a is formed to draw flue gas from the cyclones 4a,4b. The gas suction port 28a is connected to the cyclones 4a,4b, via a communicating tube 29. Fixedly secured on the upper part of the outer cylinder 28 is a cylindrical shroud 26 whose outer diameter is smaller than the inner diameter of the upper edge of the inner funnel 27. As is illustrated in FIGURE 3, the lower-end peripheral edge of the shroud 26 lies at the same level as the upper-end peripheral edge of the inner funnel 27. The lower-end peripheral edge of the shroud 26 and the upper-end peripheral edge of the inner funnel 27 define a clearance 29a through which flue gas, which has flowed into the outer cylinder 28, is introduced into the inner funnel 27. The dimension δ of this clearance 29a will next be described. The flow rate V 1 of flue gas through the communicating tube 29 can be expressed by the following formula: V 1 = A 29 x ν 29 where A 29 : cross-sectional area of the communicating tube 29, and ν29: flow velocity of flue gas through the communicating tube 29. Further, the area of the clearance 29a can be expressed by π(d 2 2 - d 1 2 )/4 = π(δ 2 + d 1 δ) , with ( d 2 - d 1 = 2δ ) where d 1 is the outer diameter of the lower end of the shroud 26 and d 2 is the inner diameter of the upper end of the inner funnel 27. The flow rate V 2 through the clearance 29a can therefore be expressed by the following formula: V 2 = π(δ 2 + d 1 δ) x νδ where νδ: flow velocity of flue gas through the clearance 29a. Since the flue gas flow rate V 1 through the communicating tube 29 and the flue gas flow rate V 2 through the clearance 29a must be equal to each other, V 1 = V 2 . From the formulae (1) and (2), the following formula can be derived: A 29 x ν 29 = π(δ 2 + d 1 δ) x νδ In the formula (3), the value of the right side can be determined basically by the flow rate of flue gas from the boiler 1. However, the outer diameter d 1 of the lower end of the shroud 26 and the flow velocity νδ of flue gas through the clearance 29a, both of which are variables, must be determined in view of various parameters such as the temperature and pressure for liquefying gaseous contaminants in flue gas and the amount of fine solid particles in the flue gas so that standard values cannot be indicated. Consequently, to determine the dimension δ of the clearance 29a, it is necessary to conduct various tests. As is shown in FIGURE 2, the three jet nozzles 30a,30b,30c are arranged at equal angular intervals on the circular periphery of the shroud 26 and the jetting direction of each of the jet nozzles 30a,30b,30c is directed in a tangential direction relative to the inner peripheral wall of the inner funnel 27. In addition, the jetting angle of each of the jet nozzles 30a,30b,30c is set such that, in FIGURE 2, the outermost boundary of the jetted air indicated by a broken line substantially reaches the adjacent jet nozzle. The duct cross-sectional area of the "B-Line" from the blower 3 to the cyclones 4a,4b is set at about "3X/4 - X/2" where X is the duct cross-sectional area of the "A-Line" from the cooler 2 to the blower 3. This is to increase the flow velocity through the "B-Line" so that a sufficient flue gas flow rate can be ensured for the cyclones 4a,4b. The duct cross-sectional area of the "B-Line" was determined by conducting tests. Between the cyclones 5a,5b arranged on the downstream side of the cyclones 4a,4b and the force feed screw 17, rotary valves 16a,16b are provided to prevent the flue gas in the first auxiliary cyclones 5a,5b from directly flowing into the force feed screw 17. The "C1-Line" is connected to the first auxiliary cyclones 5a,5b to return the flue gas to the "A-Line" again. The second auxiliary cyclones 7a,7b are provided in the "C1-Line". Provided downstream of the second auxiliary cyclones 7a,7b are the third auxiliary cyclones 8a,8b which are both connected to the force feed screw 17. To the discharge port 27a of each of the flue gas treatment apparatuses 15a,15b, a communicating tube 22 is connected to guide to the fourth auxiliary cyclone 9 fine solid particles and flue gas discharged through the discharge port 27a. The fifth auxiliary cyclone 10 connected to the force feed screw 17 is provided downstream of the fourth auxiliary cyclone 9. The blower 3, cyclones 4a,4b, first auxiliary cyclones 5a,5b, second auxiliary cyclones 7a,7b, third auxiliary cyclones 8a,8b, force feed screw 17, flue gas treatment apparatuses 15a,15b, fourth auxiliary cyclone 9, fifth auxiliary cyclone 10 and compressor 21 make up a single system. In the present embodiment, two systems are provided in parallel with the boiler 1. This was designed to improve the treatment ability of flue gas. If the amount of flue gas increases, it is necessary to provide more systems. It is to be noted that, in the present embodiment, the blower 3, force feed screw 17, fourth auxiliary cyclone 9, fifth auxiliary cyclone 10 and compressor 21 are used commonly for the individual systems. To a desired position of the force feed screw 17, the "E-Line" is connected to discharge flue gas remaining in the force feed screw 17. The blower 11 and multi-cyclone 12 are provided downstream of the "E-Line". To the multi-cyclone 12, the "F-Line" is connected to guide flue gas from the multi-cyclone 12 to the sixth auxiliary cyclone 13. In addition, a vent tube 12a is provided in the upper part of the multi-cyclone 12 in order to release the cleaned flue gas. The seventh auxiliary cyclone 14 is provided downstream of the sixth auxiliary cyclone 13. Operation of the present embodiment will next be described. Flue gas from the boiler 1 is cooled by the cooler 2 and then fed to the cyclones 4a,4b through the "A-Line", the blower 3 and the "B-Line". Fine solid particles of about 1 µm and greater are collected within the cyclones 4a,4b and are downwardly fed together with a portion of the flue gas to the first auxiliary cyclones 5a,5b. In the first auxiliary cyclones 5a,5b, second auxiliary cyclones 7a,7b and third auxiliary cyclones 8a,8b, fine solid particles are collected further from the flue gas so fed and are fed to the force feed screw 17. On the other hand, fine solid particles smaller than about 1µm are not collected in the cyclones 4a,4b but are fed together with the flue gas into the outer cylinders 28 of the flue gas treatment apparatuses 15a,15b via the communicating tubes 29. The flue gas inside each outer cylinder 28 is drawn into the inner funnel 27 through the clearance 29a by virtue of compressed air jetted out through the jet nozzles 30a,30b,30c. The pressure and flow rate of the compressed air are controlled in view of the temperature inside the inner funnel 27, the size of the inner funnel 27 and the like. This control is effected to retain a temperature required to liquefy gaseous contaminants, which are contained in the flue gas, in the inner funnel 27 and also to have an eddy current, which is formed inside the inner funnel 27, and substantially ceases at the discharge port 27a to avoid vibrations. The pressure of the compressed air is controlled at about 0,045-0,07 MPa (4.5-7.0 kg/cm 2 ) in the present embodiment. Inside the inner funnel 27, the pressure of the environment rises to a particular pressure owing to the introduction of compressed air and the temperature drops to a specific temperature. This temperature drop is caused by adiabatic expansion of the compressed air and also by effects inherent to cyclones. Owing to the pressure rise and temperature drop inside the inner funnel 27, the gaseous contaminants in the flue gas are liquefied and then adsorbed on fine solid particles in the flue gas. In the course of their turning, progressive descent under the action of the compressed air, the fine solid particles are subjected to centrifugal force and are hence separated from the flue gas. When the flue gas enters the inner funnel 27, water vapor in the flue gas is condensed into water because of the temperature drop of the flue gas. Water is also formed upon production of the compressed air. Fine solid particles are therefore adsorbed on these water molecules. This makes it possible to collect fine solid particles having substantially small particle sizes so that the collection efficiency for fine solid particles can be improved. The remaining flue gas and the like are introduced into the fourth auxiliary cyclone 9 and fifth auxiliary cyclone 10, where the fine solid particles with air pollutants adsorbed thereon are separated from the remaining flue gas and are discharged to the force feed screw 17. As has been described above, the present embodiment can remove gaseous and fine solid particulate contaminants from flue gas without any chemical facility, thereby reducing both the running costs and initial costs. Inside the flue gas treatment apparatuses 15a,15b, deodorization making use of fine solid particles is also effected in addition to the treatment for the removal of fine solid particulate and gaseous contaminants. Unburnt carbon is contained in flue gas from a combustion equipment like the boiler 1. This unburnt carbon conducts deodorization. The deodorization inside the flue gas treatment apparatuses 15a,15b promptly proceeds as the pressure of the atmosphere is elevated and unburnt carbon is contained in the form of fine particles of about 1µm and smaller. The remaining flue gas from which fine solid particulate and gaseous contaminants have been substantially removed reaches the blower 11 from the fourth auxiliary cyclone 9 via the "D-Line" and the "E-Line" and is then blown into the multi-cyclone 12. Final dust collection is conducted in the multi-cyclone 12. Fine solid particles are fed to the force feed screw 17 via a rotary valve 16c and the flue gas so cleaned is released through the vent tube 12a. In this embodiment, the plural flue gas treatment apparatuses 15a,15b and the plural auxiliary cyclones 5a,7a,... are provided. The number of these equipments should be determined depending on the amount of flue gas to be produced and the degree of its contamination and shall not be construed as limiting the present invention. The second embodiment of this invention will next be described with reference to FIGURE 6 and FIGURE 7. In this embodiment, as is depicted in FIGURE 6, an auxiliary line is provided above the two flue gas treatment apparatuses 15a,15b, in other words, to free ends of the shut-off valves 25, and the auxiliary line terminates in a dust removing filter 60 so that flue gas can be returned again to the flue gas treatment apparatus 15a. To introduce a portion of the flue gas, which has been fed into the flue gas treatment apparatuses 15a,15b, into the dust removing filter 60 and also to force the flue gas to return again from the dust removing filter 60 to the flue gas treatment apparatus 15a, blowers 61,62 are provided in this embodiment. The remaining construction is similar to the corresponding construction in the first embodiment. In general, the amount of flue gas produced in the boiler 1 is not constant. The provision of the dust removing filter 60 in this embodiment is, therefore, to open the shut-off valves 25 of the flue gas treatment apparatuses 15a,15b when the flue gas treatment apparatuses 15a,15b cannot treat all of the flue gas, whereby any extra flue gas can be treated by the dust removing filter 60. Since the basic construction of this embodiment is substantially the same as that of the first embodiment, its advantages are practically similar to those of the first embodiment except for the advantage described above. Flue gas produced when used tires were burnt in the boiler 1 was treated using the system of this embodiment. Various measurements were carried out to determine the effects of the treatment. This will be described with reference to FIGURE 7. As is shown in the same figure, the concentration of soot and dust dropped from 16.2 g/m 3 N at the entrance of the system to 0.02 g/m 3 N at the exit of the system. Such significant soot-and-dust-removing effects are believed to be attributed to very effective collection by water, which has been formed as a result of liquefaction of water vapor contained in the flue gas, in addition to centrifugal removal in the flue gas treatment apparatuses 15a,15b and the various cyclones 5a,5b,7a,... as described above. Further, the concentration of sulfur oxides dropped from 562 ppm by volume at the entrance of the system to 15 ppm by volume at the exit of the system. Regarding nitrogen oxides, their concentration dropped from 37 ppm by volume at the entrance to 15 ppm by volume at the exit of the system. In addition, removing effects were also observed with respect to hydrogen chloride, hydrogen sulfide, methyl sulfide and the like. Incidentally, the concentrations of sulfur oxides, nitrogen oxides and hydrogen chloride were within their respective environmental quality standards. The soot and dust so recovered had the following compositions: 1.66 mg/kg As, 0.024 mg/kg T-Hg (the content of mercury including various mercury compounds), 3080 mg/kg Pb, 14.9 mg/kg Cd, 53.0 mg/kg T-Cr (the content of chromium including all chromium compounds), 1.08% SiO 2 , 21.1 mg/kg CN, less than 0.0005 mg/kg PCB, less than 0.05 mg/kg O-P (organophosphorus), 36% C and 49.1% water. As has been demonstrated above, this embodiment and the other embodiments can efficiently remove fine solid particles, namely, soot and dust and can also eliminate various air pollutants. The different embodiments of the present invention have been described above. In these embodiments, the boiler was exemplified as a flue gas source. The present invention is not limited to boilers but can be applied to any equipments as long as they produce flue gas, for example, diesel engines of ships, vehicles and the like, reactors in chemical plants, garbage incinerators, and so on.

Claims: Flue gas treatment apparatus (15a, 15b) which comprises: a closed funnel (27), with an upper shroud (26) an inlet portion (29a) for drawing flue gas provided in the upper part of the funnel (27), one or several jet nozzles (30a,30b,30c) for jetting out a compressed gas, preferably air, along the upper inner peripheral wall of the funnel (27), and a discharge port (27a) provided in the lower part of the funnel (27). The apparatus according to claim 1, characterized in that an outer cylinder (28) is provided enclosing at least the upper part of the funnel (27), and the inlet portion is a clearance (29a) formed between the upper-end peripheral edge of the funnel (27) and the lower-end peripheral edge of the shroud (26). The apparatus according to claim 2, characterized in that a gas suction port (28a) is provided between the inner wall of the outer cylinder (28) and the outer wall of the funnel (27) in its lower part. The apparatus according to one or several of claims 1 to 3, characterized by one or more of the following features: an odd number of jet nozzles (30a,30b,30c) are provided, the jet nozzles (30a,30b,30c) are arranged at equal angular intervals on the circular periphery of shroud (26), the jet nozzles (30a,30b,30c) are arranged such that the jetting direction is tangential relative to the inner peripheral wall of the funnel (27) and the jetting angle of each of the jet nozzles (30a,30b,30c) is set such that the outermost boundary of the jetted air substantially reaches the adjacent jet nozzle. Flue gas treatment system, comprising: a flue gas treatment apparatus according to one of claims 1 to 4, the inlet portion (29a) of which is connected to a flue gas source (1) and a source (21) of compressed gas for feeding it to the jet nozzles (30a, 30b,30c). The system according to claim 5, wherein a plurality of flue gas treatment apparatus (15a,15b) are provided in series connection and/or parallel with the flue gas source (1). The system according to claim 5 and/or 6, wherein one or more cyclone dust collectors (4a,4b,9) are provided on the upstream and/or downstream side of the flue gas treatment apparatus (15a,15b). The system according to one or several of claims 5 to 7, characterized in that a gas cooler (2) is provided to cool the flue gas before it flows into the flue gas treatment apparatus (15a,15b). Process for the treatment of flue gas containing fine solid particles, characterized in that the flue gas is introduced into the upper part of a funnel with an upper shroud together with a compressed, jetted out gas, preferably air, along the upper inner peripheral wall of the funnel, forming an eddy current, such that the pressure rises as a result of the introduction of the compressed air, and the temperature is decreased because of adiabatic expansion of the compressed gas, and liquid water is formed, which is discharged from the lower part of the funnel together with fine solid particles. The process according to claim 9, characterized in that an apparatus according to one of claims 1 to 4 or a system according to one of claims 5 to 8 is used.

Inventors: YANG YUN SEUK, YANG, YUN, SEUK, YANG, YUN, SEUK, 110-207, JUCO APARTMENT
Applicants: SANKO IND CORP, SANKO INDUSTRIES CORPORATION
Application year: 1991
Main classification: B01D53
IPC codes: B01D53, B04C5, B04C9, B01D45, F01N3