Automatic feeding system of catalyst for solid pretreatment desulfurization

Abstract

According to one embodiment of the present invention, the automatic introduction system for a solid pretreatment desulfurization catalyst comprises: a main silo in which a plurality of lower end discharge ports are formed and which receives the introduction of a solid pretreatment desulfurization catalyst from an open upper end introduction port; and a plurality of metering silos which are located below the main silo, receive the supply of coal from respective discharge ports at the lower end of the main silo, and, in a state in which the metering silos are respectively disposed above a coal supply conveyor of a thermal power plant, drop a catalyst for solid pretreatment desulfurization to the upper part of the coal transferred by the coal supply conveyor, and discharge the coal from the discharge ports at the lower end of the main silo. The solid pretreatment desulfurization catalyst is introduced into the transferred coal; and a sensing control unit for sensing the amount of coal fed by the coal feed conveyor, and for controlling the opening and closing of the discharge ports of the metering silos in conjunction with the sensed amount of coal fed, respectively, and for controlling the opening and closing of the discharge ports of the metering silos in conjunction with the sensed amount of coal fed by the coal feed conveyor. Therefore, the catalyst for solid pretreatment desulfurization is controlled to fall and be fed according to a certain proportion in a manner of being in direct proportion to the feeding amount of coal.

Description

Technical Field

[0001] The present invention relates to an automatic input system for a solid pretreatment desulfurization catalyst, and more particularly to an improved automatic input system for a solid pretreatment desulfurization catalyst that can be automatically and quantitatively input into the coal supply of a thermal power plant. The solid pretreatment desulfurization catalyst is obtained by impregnating a liquid pretreatment desulfurization catalyst into a carrier having pores and then drying it to solidify, thereby not only minimizing the weight of the desulfurization catalyst, but also simplifying the manufacturing engineering equipment, and further improving the storage stability and logistics cost. Background Art

[0002] Sulfur oxides (SOx) and nitrogen oxides (NOx) are important pollution sources that induce air pollution. In particular, sulfur oxides are contained in industrial waste gases released during the combustion of fossil fuels containing sulfur components, which can cause various environmental pollution problems such as acid rain.

[0003] For a long time, people have been committed to researching desulfurization methods that can remove sulfur oxides from the above-mentioned industrial exhaust gases. In factories or power plants using fossil fuels, post-combustion treatment methods, i.e., flue gas desulfurization methods, are usually adopted.

[0004] The flue gas desulfurization method refers to a method of desulfurizing the exhaust gas after burning fossil fuels containing sulfur gas. The above-mentioned flue gas desulfurization method can be divided into a wet method and a dry method. The wet method refers to a method of removing sulfur oxides by washing the exhaust gas with, for example, ammonia water, sodium hydroxide solution, and lime milk, while the dry method refers to a method of adsorbing or reacting sulfur dioxide by contacting particles or powders such as activated carbon and carbonates with the exhaust gas and thereby removing sulfur oxides.

[0005] However, in order to use the flue gas desulfurization method, there are problems such as the need to separately construct desulfurization equipment for treating exhaust gas, and the need to consume a large amount of manpower and cost during the operation of the desulfurization equipment and the complexity of the desulfurization process.

[0006] Therefore, in order to reduce the emissions of sulfides related to the combustion of fossil fuels, it is urgent to carry out research on pretreatment desulfurization catalysts and desulfurization methods that can be pre-mixed with fuels before fuel combustion and can simultaneously perform desulfurization during the fuel combustion process.

[0007] As an example of the above-mentioned pretreatment desulfurization catalyst, it includes Patent Registration No. 1864999 (hereinafter referred to as the "previous application patent") applied by the applicant of the present invention.

[0008] In the aforementioned prior patent application, a liquid pretreatment desulfurization catalyst that can be simply and easily applied during the combustion of fossil fuels and has excellent desulfurization effects, a method for manufacturing the desulfurization catalyst, and a desulfurization method using the desulfurization catalyst were disclosed.

[0009] However, the aforementioned liquid pretreatment desulfurization catalyst still has the following problems.

[0010] First, the existing liquid pretreatment desulfurization catalyst is manufactured in a liquid state by mixing a liquid raw material with water or the like. Therefore, its manufacturing engineering equipment is complex, and due to the characteristics of liquid chemical substances, its storage stability is poor. Moreover, because it is in a liquid form, it must be transported using a tanker truck equipped with a special container, resulting in an increase in its logistics cost and storage cost.

[0011] Second, when the existing liquid pretreatment desulfurization catalyst is mixed into a combustible material such as coal or oil for pretreatment, for example, a separate device for spraying is required, resulting in an increase in the cost burden of the manufacturing engineering equipment.

[0012] Third, when the existing liquid pretreatment desulfurization catalyst is added to coal in large quantities, for example, it may cause the problem of clogging the coal inlet due to the gelation of coal, or the problem of flowing downward in the form of slurry together with coal on the conveyor belt for transporting coal.

[0013] For the reasons described above, there is an urgent need to develop and popularize an improved solid pretreatment desulfurization catalyst that can minimize the weight of the desulfurization catalyst by solidifying the existing liquid pretreatment desulfurization catalyst into a stable solid form, simplify the manufacturing engineering equipment, and improve the storage stability and logistics cost. Summary of the Invention

[0014] Therefore, the present invention aims to solve the above problems, and its object is to provide an improved automatic feeding system for a solid pretreatment desulfurization catalyst that solidifies a liquid pretreatment desulfurization catalyst by impregnating it into a carrier having pores and then drying it, so as to not only minimize the weight of the desulfurization catalyst, simplify the manufacturing engineering equipment, but also improve the storage stability and logistics cost, and is intended to automatically quantitatively feed the solid pretreatment desulfurization catalyst into the coal supply of a thermal power plant.

[0015] To achieve the above object, an embodiment of the automatic feeding system of the catalyst for solid pretreatment desulfurization according to the present invention includes: a main silo formed with a plurality of lower discharge ports, receiving the supply of the catalyst for solid pretreatment desulfurization from the open upper inlet; a plurality of metering silos located below the main silo, receiving the supply of coal from each of the discharge ports at the lower end of the main silo, and in a state of being respectively disposed above the coal supply conveyor in a thermal power plant, causing the catalyst for solid pretreatment desulfurization to fall onto the upper part of the coal transported by the coal supply conveyor, so as to feed the catalyst for solid pretreatment desulfurization into the transported coal; and a sensing and control unit, sensing the input amount of the coal transported by the coal supply conveyor, and controlling the opening and closing of the discharge ports of the metering silos in a manner linked to the sensed input amount of the coal, so as to control the catalyst for solid pretreatment desulfurization to fall and be fed in a certain proportion in direct proportion to the coal input amount.

[0016] In addition, in one embodiment, on one side of the main silo, it further includes: a vertical transfer assembly for vertically transferring the catalyst for solid pretreatment desulfurization from the ground to the upper inlet of the main silo.

[0017] In addition, in one embodiment, it is characterized in that: the vertical transfer assembly is a bucket elevator or a hoist.

[0018] In addition, in one embodiment, at least one position between the discharge port of the main silo and the inlet of the metering silo or between the discharge port of the metering silo and the coal supply conveyor further includes: a horizontal transfer assembly for horizontally transferring the catalyst for solid pretreatment desulfurization.

[0019] In addition, in one embodiment, it is characterized in that: the horizontal transfer assembly is a screw feeder or a belt conveyor.

[0020] In addition, in one embodiment, on the outer surface adjacent to the discharge port of the main silo, it further includes: at least one vibrator for applying vibration to prevent the stagnation of the catalyst for solid pretreatment desulfurization discharged through the discharge port of the main silo.

[0021] In addition, in one embodiment, at the discharge port of the main silo or the metering silo, it further includes: a rotary valve for controlling the discharge of the catalyst for solid pretreatment desulfurization.

[0022] In addition, in one embodiment, the sensing control unit includes: a load cell disposed at the lower end of the coal supply conveyor to measure the instantaneous weight of the supplied coal; and a motion detector disposed above the coal supply conveyor to measure the transfer speed of the transferred coal supply.

[0023] In addition, in one embodiment, the metering silo inputs the solid pretreatment desulfurization catalyst into the supplied coal at a ratio of 0.1 to 0.5 wt% per hour compared to the weight of the coal supply transferred on the coal supply conveyor.

[0024] In addition, in one embodiment, the manufacture of the solid pretreatment desulfurization catalyst includes: (a) a step of manufacturing a liquid pretreatment desulfurization catalyst; (b) a step of crushing a carrier having a porous structure with pores into a certain size; (c) a step of immersing the carrier crushed into a certain size in the step (b) into the liquid pretreatment desulfurization catalyst manufactured in the step (a) and impregnating for 10 to 60 minutes; and (d) a step of drying the carrier at a temperature of 100 °C or higher for a certain time after putting the carrier into a dryer in a state where the liquid pretreatment desulfurization catalyst has penetrated into the pores of the carrier through the impregnation in the step (c).

[0025] In addition, in one embodiment, after the step (d), it further includes: (e) a step of pulverizing the carrier dried in a state where the liquid pretreatment desulfurization catalyst has penetrated into the pores of the carrier into powder.

[0026] In addition, in one embodiment, after the step (e), it further includes: (f) a step of using the solid component manufactured into powder through the step (e) as the solid pretreatment desulfurization catalyst, or putting the solid component into an extruder to manufacture pellets, or putting the solid component into a tablet press to manufacture tablets.

[0027] As described above, the automatic input system of the solid pretreatment desulfurization catalyst of the present invention can, after being automatically quantitatively input as a pretreatment into the coal supply of a thermal power plant, activate its porosity by adsorbing to the ash generated in the combustion particles during the combustion process of the combustibles, and efficiently adsorb and remove sulfur oxides (SOx) present in the ash, thereby achieving the excellent effect of reducing the emission amount of sulfur oxides before the generation of exhaust gas.

[0028] In addition, during the movement of the coal supply on the conveyor, the catalyst for solid pretreatment desulfurization is mixed in a certain proportion above the conveyor in a manner linked to the weight of the coal supply. Therefore, it is simpler and easier to input compared with the existing liquid desulfurization catalyst, and since there is no flow of the liquid desulfurization catalyst, it can be easily applied to various combustion facilities, thereby achieving the effect of effectively reducing the emissions of sulfur oxides (SOx) caused by the combustion of fossil fuels before the exhaust gas is discharged.

[0029] In addition, the desulfurization system according to the present invention does not require a separate desulfurization treatment facility for treating the exhaust gas generated after the combustion of the combustible. Instead, by burning after mixing the combustible with the solid pretreatment desulfurization catalyst, the economic effect of rapidly reducing sulfur oxides at a low cost can be achieved. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 It is a flowchart for explaining the manufacturing method of the solid pretreatment desulfurization catalyst applicable to the present invention.

[0031] Figure 2 It is an illustrative diagram showing the overall configuration of the automatic input system of the solid pretreatment desulfurization catalyst of the present invention.

[0032] Figure 3 is Figure 2 plan view. DETAILED DESCRIPTION OF THE INVENTION

[0033] The terms used in this specification are only for explaining specific embodiments and are not intended to limit the present invention. Unless there is a clear contrary meaning in the context, a singular statement also includes a plural meaning. In this specification, terms such as "including", "having", or "equipped with" are only used to indicate the existence of the features, numbers, steps, actions, components, parts, or combinations described in this specification, and should not be construed as precluding the possibility of the existence or addition of one or more other features, numbers, steps, actions, components, parts, or combinations.

[0034] Unless otherwise defined in this specification, all terms used herein, including technical or scientific terms, have the same meaning as commonly understood by those of ordinary skill in the technical field to which the present invention pertains.

[0035] Terms that are commonly used and defined in a dictionary should be interpreted as having a meaning consistent with their meaning in the context of the related art, and should not be interpreted as idealized or overly formal meanings unless clearly defined in this specification.

[0036] Next, an embodiment of the manufacturing method of the catalyst for solid pretreatment desulfurization applicable to the present invention will be specifically described with reference to the accompanying drawings.

[0037] Figure 1 It is a flowchart for explaining the manufacturing method of the catalyst for solid pretreatment desulfurization of the present invention.

[0038] First, refer to Figure 1 , the manufacturing process of the catalyst for solid pretreatment desulfurization applicable to the present invention may include the following steps in one embodiment.

[0039] Step (a): Manufacture a liquid catalyst for pretreatment desulfurization (S100).

[0040] The liquid catalyst for pretreatment desulfurization according to the present invention can be manufactured according to the following specific steps in one embodiment.

[0041] Step (a-1): Mix and micronize one or more oxide powders selected from the group consisting of SiO2, Al2O3, Fe2O3, TiO2, MgO, MnO, CaO, Na2O, K2O, and P2O3.

[0042] Step (a-2): Mix and micronize one or more metal powders selected from the group consisting of Li, Cr, Co, Ni, Cu, Zn, Ga, Sr, Cd, and Pb.

[0043] Step (a-3): Form a desulfurization catalyst by mixing the oxide in step (a-1) and the metal in step (a-2) with one or more liquid compositions selected from the group consisting of sodium tetraborate (Na2B4O7·10H2O), sodium hydroxide (NaOH), sodium silicate (Na2SiO3), and hydrogen peroxide (H2O2).

[0044] Step (a-1) is a step of mixing one or more oxide powders selected from the group consisting of SiO2, Al2O3, Fe2O3, TiO2, MgO, MnO, CaO, Na2O, K2O, and P2O3 and micronizing them by a micronizer.

[0045] In this step, the oxide powder may contain 15-90 parts by weight of SiO2, 15-100 parts by weight of Al2O3, 10-50 parts by weight of Fe2O3, 5-15 parts by weight of TiO2, 20-150 parts by weight of MgO, 10-20 parts by weight of MnO, 20-200 parts by weight of CaO, 15-45 parts by weight of Na2O, 20-50 parts by weight of K2O, and 5-20 parts by weight of P2O3.

[0046] In addition, in this step, the particle size of the micronized oxide powder can reach 1 - 2 μm by repeatedly performing micronization.

[0047] The step (s-2) is a step of mixing one or more metal powders selected from the group consisting of Li, Cr, Co, Ni, Cu, Zn, Ga, Sr, Cd, and Pb and micronizing them with a micronizer.

[0048] In this step, the metal powder may contain 0.0035 - 0.009 parts by weight of Li, 0.005 - 0.01 parts by weight of Cr, 0.001 - 0.005 parts by weight of Co, 0.006 - 0.015 parts by weight of Ni, 0.018 - 0.03 parts by weight of Cu, 0.035 - 0.05 parts by weight of Zn, 0.04 - 0.08 parts by weight of Ga, 0.02 - 0.05 parts by weight of Sr, 0.002 - 0.01 parts by weight of Cd, and 0.003 - 0.005 parts by weight of Pb.

[0049] In addition, in this step, the particle size of the micronized metal powder can reach 1 - 2 μm by repeatedly performing micronization.

[0050] In the step (a-3), a liquid pretreatment desulfurization catalyst is formed by mixing the oxide powder and the metal powder that are mixed and micronized in the step (a-1) and the step (a-2) with one or more liquid compositions selected from the group consisting of sodium tetraborate (Na2B4O7·10H2O), sodium hydroxide (NaOH), sodium silicate (Na2SiO3), and hydrogen peroxide (H2O2).

[0051] In this step, the liquid composition may contain 20 - 130 parts by weight of sodium tetraborate (Na2B4O7·10H2O), 15 - 120 parts by weight of sodium hydroxide (NaOH), 50 - 250 parts by weight of sodium silicate (Na2SiO3), and 10 - 50 parts by weight of hydrogen peroxide (H2O2).

[0052] In addition, when reacting by mixing with the oxide powder and the metal powder that are mixed and micronized in the step (a-1) and the step (a-2) in this step, the oxide powder and the liquid composition will act as chelating agents, so that a chelation reaction can occur with the metal powder to form a metal chelate compound.

[0053] In addition, the liquid pretreatment desulfurization catalyst formed in this step is stabilized by precipitation for 24 to 72 hours. It can be used as a powdered desulfurization catalyst in powder form by separating the precipitated desulfurization catalyst and drying it naturally. Alternatively, the liquid composition remaining after separating the precipitated desulfurization catalyst can be used as the liquid pretreatment desulfurization catalyst of the present invention.

[0054] Among them, the precipitate of the precipitated liquid desulfurization catalyst is naturally dried and named the powdered desulfurization catalyst (GTS-P). Furthermore, the liquid composition after separating the precipitated powder composition is transferred to a separate container and named the liquid pretreatment desulfurization catalyst (GTS).

[0055] For reference, the powdered desulfurization catalyst (GTS-P) can be solidified by naturally drying the precipitate of the liquid pretreatment desulfurization catalyst (GTS) in the manner described above. However, in the above-mentioned case, various problems as described below occurred.

[0056] First, because GTS-P has high viscosity, it not only has the problem of extremely slow drying speed but also the problem of difficult internal drying due to the solidification of the skin part. Therefore, when the drying temperature is increased to dry GTS in an aqueous solution state, it will exist in a highly viscous liquid state due to its high solubility in water, resulting in a complicated manufacturing process.

[0057] Second, after drying, corrosion occurred in the metal material equipment, and the problem of GTS attachments forming on the wall surface of the equipment also occurred. In addition, when stored in a general atmospheric state, the storage safety deteriorates due to moisture absorption. Moreover, the powdered solid of GTS-P that has only been simply dried will quickly liquefy due to moisture absorption from the air when dispersed in coal, resulting in complicated addition methods and equipment. Due to the reasons described above, the powdered desulfurization catalyst (GTS-P) is not suitable for use as the solid pretreatment desulfurization catalyst of the present invention.

[0058] Therefore, the liquid pretreatment desulfurization catalyst (GTS), which is one of the main materials of the present invention, is manufactured and prepared through the above steps (a-1) to (a-3).

[0059] Step (b): Crush the carrier with a porous structure having pores into a certain size (S200).

[0060] In one embodiment, porous materials such as expanded vermiculite, perlite, diatomaceous earth, and activated carbon are used as the carrier. The apparent specific gravity of the carrier used is 0.1 to 0.5, the water absorption rate is 60 to 300 cc / 100 g, and the particle size is 10 to 2,000 μm.

[0061] The carrier is preferably a material having a porous structure. Moreover, since a large number of pores in the carrier have the ability to maintain moisture, components that play a desulfurization role can be appropriately contained in the solid phase. In addition, because of its air permeability, sodium sulfate (Na2SO4) can be generated by reacting with sulfur oxides. In particular, because of its heat insulation characteristics, the decomposition reaction in the high-temperature region can be prevented. Generally speaking, at temperatures above 1200 °C, the decomposition reaction of sodium sulfate may occur to generate sulfur oxides and be discharged as exhaust gas, resulting in a problem of decreased desulfurization performance. In addition, since there are desulfurization components with strong alkaline properties in the porous material, it can act as a three-dimensional obstacle to minimize the attachment of strong alkaline components to the inner wall of the combustion furnace, thereby avoiding high-temperature corrosion caused by the attachment of alkaline substances to the inner wall of the combustion furnace. In particular, for expanded vermiculite with a plate-like structure, it has the advantage of being more conducive to solid-liquid impregnation because of its faster water absorption rate.

[0062] Step (c): Immerse the carrier crushed to a certain size in the liquid pretreatment desulfurization catalyst prepared in the step (a) and impregnate for 10 to 60 minutes (S300).

[0063] In one embodiment, the liquid pretreatment desulfurization catalyst (GTS) and the vermiculite carrier can be mixed in a mass ratio range of 5:1 to 20:1, and more preferably, they can be mixed in a mass ratio of 10:1.

[0064] Regarding the time for impregnating the liquid pretreatment desulfurization catalyst (GTS) into the vermiculite carrier, impregnation is performed for at least 1 hour so that the liquid pretreatment desulfurization catalyst can be fully impregnated between the pores of the vermiculite carrier.

[0065] Step (d): After the carrier is put into a dryer in a state where the liquid pretreatment desulfurization catalyst penetrates into the pores of the carrier through the impregnation in the step (c), drying is performed at a temperature of 100 °C or higher for a certain period of time (S400).

[0066] In addition, in one embodiment, the step (d) can be composed of the following specific steps.

[0067] Step (d-1): After the carrier impregnated with the liquid pretreatment desulfurization catalyst is put into the dryer, the internal temperature of the dryer is raised from room temperature to 130 °C, and then the first drying is carried out for 2 hours.

[0068] Step (d-2): After the carrier that has undergone the first drying in the above step (d-1) is heated to 230 °C, the second drying is carried out for 2 - 3 hours.

[0069] By performing multi-stage drying within a sufficient drying time in the manner of the first drying of raising the temperature from room temperature to 130 °C and then drying, and the second drying of raising the temperature from 130 °C to 230 °C and then drying as described above, it can be confirmed that the hot air is evenly penetrated into the interior of the porous structure and thus uniform drying is achieved. In addition, through the drying test described later, it can be confirmed that in the resultant product after the second drying, the moisture content of the carrier impregnated with the liquid pretreatment desulfurization catalyst is less than 5%.

[0070] In addition, in another embodiment, even when the first and second drying processes of the above-described embodiment steps (d-1) and (d-2) are not performed, but only the second drying of step (d-2) for 160 minutes is carried out, a moisture content of less than 5% can also be achieved.

[0071] In addition, in the above-described one embodiment and another embodiment, when a drum-type powder dryer is used as the dryer, since the carrier is dried while performing a rolling motion in the drum-type drying barrel, the drying time can be further reduced, which is more conducive to the continuous production of the solid pretreatment desulfurization catalyst according to the present invention.

[0072] Step (e): After drying in a state where the liquid pretreatment desulfurization catalyst penetrates into the pores of the carrier, the carrier is put into a pulverizer and pulverized into a certain size (S500).

[0073] Regarding the pulverized size, the solid component can be pulverized into particle sizes of 10 mesh (1.9 mm) or less by a pulverizer, but it can also be pulverized into an appropriate size according to the type of combustible material and the mixing method. Thus, the solid component manufactured in powder form as described above can be directly used as the solid pretreatment desulfurization catalyst (first form) of the present invention.

[0074] Step (f): The solid component manufactured into powder through the above step (e) is put into an extruder to manufacture pellets (pellet, second form), or the solid component is put into a tablet press to manufacture tablets (Tablet, third form) (S600).

[0075] As described above, the solid pre-treatment desulfurization catalyst of the present invention (hereinafter referred to as "GTS-S") processed into powder (first form), granule (second form) or tablet (third form) is finally manufactured through the above steps (a) to (f).

[0076] That is, the dried product manufactured into powder can be shipped as a GTS-S product, or various forms of GTS-S products can be manufactured by processing into pellet form using an extruder or processing into tablets using a tablet press after crushing into granules with a particle size of 10 mesh (1.9 mm) or less using a crusher. At this time, in one embodiment, the size of the granules or tablets manufactured in the above-described manner can be manufactured to have a diameter of 2 mm to 50 mm and a ratio of length to diameter (L / D) of 1 or less.

[0077] In addition, the desulfurization method using the solid pre-treatment desulfurization catalyst applicable to the present invention is characterized in that: the solid pre-treatment desulfurization catalyst manufactured in the above-described manner is premixed with the combustible material and then burned, and sulfur oxides are adsorbed and removed through pre-treatment during the combustion process.

[0078] In addition, in one embodiment, the mixing ratio of the solid pre-treatment desulfurization catalyst mixed into the combustible material can be adjusted according to the content ratios of C, H, N, and S contained in the combustible material. For example, in the case where the combustible material is Vietnam Uong Bi 3 coal, since the sulfur content is high, the input amount of the solid pre-treatment desulfurization catalyst (GTS-S) applicable to the present invention needs to be increased, so that a larger amount is mixed compared to ordinary coal.

[0079] Next, reference will be made to Figure 2 and Figure 3 to describe the configuration of the automatic feeding system for the solid pre-treatment desulfurization catalyst of the present invention.

[0080] Figure 2 is an exemplary diagram showing the overall configuration of the automatic feeding system for the solid pre-treatment desulfurization catalyst of the present invention, and Figure 3 is Figure 2 a plan view.

[0081] First, in one embodiment of the automatic feeding system 1000 for the solid pre-treatment desulfurization catalyst of the present invention, a main silo 1300 is provided, which is formed with a plurality of lower discharge ports and receives the supply of the solid pre-treatment desulfurization catalyst (GTS-S) from the open upper input port.

[0082] In one embodiment, the case where there are two discharge ports formed at the lower ends of the two main silos 1300 is illustrated as an example, but more can also be formed. In addition, the lower end portion of the main silo 1300 is in the form of a hopper. In one embodiment, as Figure 2 and Figure 3 shown, it can be implemented in the form of a twin hopper with two (a pair of) lower discharge ports.

[0083] In addition, a metering silo 1400 is provided below the main silo 1300. Among them, multiple metering silos can be provided. In one embodiment, referring to Figure 2 and Figure 3 , two metering silos 1410 can be provided according to the number of discharge ports of the main silo 1300, that is, a first metering silo 1410 and a second metering silo 1420.

[0084] Each of the first and second metering silos 1410 and 1420 is respectively arranged above the first and second coal supply conveyors 100 and 200 that receive the supply of coal from the respective discharge ports at the lower end of the main silo 1300 and transfer the coal to the boiler of the thermal power plant. In the state as described above, the solid pretreatment desulfurization catalyst (GTS-S) will respectively fall through the discharge ports of the first and second metering silos 1410 and 1420 onto the upper part of the coal being transferred on the first and second coal supply conveyors 100 and 200, so as to input the solid pretreatment desulfurization catalyst (GTS-S) to the transferred coal in a certain proportion.

[0085] In addition, a sensing control unit for controlling the solid pretreatment desulfurization catalyst (GTS-S) to fall and be input in a certain proportion in direct proportion to the coal input amount is provided on the first and second coal supply conveyors 100 and 200.

[0086] In one embodiment, the sensing control unit may include: load cells (not shown), which are respectively provided at the lower ends of the first and second coal supply conveyors 100 and 200 to measure the instantaneous weight of the coal supply transferred to the boiler of the thermal power plant; and motion detectors 1610 and 1620, which are provided above the coal supply conveyors 100 and 200 to measure the transfer speed of the transferred coal supply.

[0087] Thereby, the load cell (not shown) can respectively sense the instantaneous weight of the coal transferred by the first and second coal supply conveyors 100 and 200, and the motion detectors 1610 and 1620 can respectively measure the hourly transfer speed of the first and second coal supply conveyors 100 and 200. Next, the instantaneous weight of the coal supply obtained in the above-described manner can be multiplied by the hourly transfer speed of the coal supply conveyor to calculate the hourly input amount of the coal.

[0088] Thereby, the discharge ports of the first and second metering silos 1410 and 1420 can be respectively opened and closed in a manner linked to the input amount of the coal calculated in the above-described manner, so as to ultimately control the input amount of the solid pretreatment desulfurization catalyst (GTS-S).

[0089] In addition, on one side of the main silo 1300, a vertical transfer assembly is provided for vertically transferring the solid pretreatment desulfurization catalyst (GTS-S) from the ground to the upper input port of the main silo 1300.

[0090] In one embodiment, the vertical transfer assembly can be one of a bucket elevator 1200 or a hoist device.

[0091] More specifically, referring to Figure 2 and Figure 3 , the bucket elevator 1200 can be used to vertically transfer the solid pretreatment desulfurization catalyst (GTS-S) from the ground to the upper input port of the main silo 1300. At this time, the solid pretreatment desulfurization catalyst (GTS-S) can be transported to the bucket elevator 1200 by a truck or the like in a state of being loaded into a ton bag, and an operator can use a separate crane 1100 to transfer and load the solid pretreatment desulfurization catalyst (GTS-S) in the ton bag into the bucket of the bucket elevator 1200.

[0092] In addition, at least one position between the discharge port of the main silo 1300 and the input ports of the first and second metering silos 1410 and 1420 or between the respective discharge ports of the first and second metering silos 1410 and 1420 and the first and second coal supply conveyors 100 and 200 is provided with a horizontal transfer assembly 1800 for horizontally transferring the solid pretreatment desulfurization catalyst (GTS-S).

[0093] In one embodiment, the horizontal transfer assembly 1800 may be one of a screw feeder or a belt conveyor. Thereby, by using the horizontal transfer assembly 1800, a horizontal connection can be made to the supply flow path of the solid pretreatment desulfurization catalyst (GTS-S) between the discharge port of the main silo 1300 and the inlets of the first and second metering silos 1410 and 1420, which are not arranged directly below but may be spaced apart from each other by a certain distance, or between the discharge ports of the first and second dosing silos 1410 and 1420 and the first and second coal supply conveyors 100 and 200.

[0094] In addition, on the outer surface adjacent to the discharge port of the main silo 1300, at least one vibrator 1700 is provided to apply vibration to prevent the solid pretreatment desulfurization catalyst (GTS-S) discharged through the discharge port of the main silo 1300 from stagnating. In one embodiment, the vibrator 1700 can be controlled to work together when the discharge port of the main silo 1300 is opened.

[0095] In addition, at the discharge ports of the main silo 1300 or the first and second metering silos 1410 and 1420, a rotary valve 1500 is provided to control the discharge of the solid pretreatment desulfurization catalyst (GTS-S). The rotary valve 1500 is a device for quantitatively supplying the solid pretreatment desulfurization catalyst (GTS-S) in powder form downward through the rotational movement of the valve. In one embodiment, referring to Figure 2 , one rotary valve 1500 can be provided at each discharge port, that is, a total of four positions 1510, 1520, 1530, and 1540 are equipped.

[0096] In one embodiment, the first and second metering silos 1410 and 1420 can control the operation of the rotary valves 1530 and 1540 provided at the discharge ports to input the solid pretreatment desulfurization catalyst (GTS-S) into the coal supply at a ratio of 0.1 to 5 wt% per hour compared to the weight of the coal supply transferred on the coal supply conveyor.

[0097] Among them, the input ratio of GTS-S in the range of 0.1 to 0.5 wt% is a value obtained by the inventors through actual measurement of coals from different origins. It can be confirmed that when the input amount of GTS-S is less than 0.1 wt% per hour, the sulfur oxide reduction efficiency of the coal decreases, and when the input amount exceeds 0.5 wt%, the sulfur oxide reduction efficiency of the coal no longer increases, resulting in waste of GTS-S.

[0098] Next, assuming that the automatic feeding system for the catalyst for solid pretreatment desulfurization of the present invention configured as described above is installed in a thermal power plant, the process of calculating the feeding amount of the catalyst for solid pretreatment desulfurization (GTS-S) will be described.

[0099] 1. Coal feeding amount of the thermal power plant (transfer amount of the coal conveyor): at least 130 tons (ton) to 250 tons per hour

[0100] 2. Feeding ratio of GTS-S: 0.1 to 0.5 wt% per hour compared to the coal feeding amount

[0101] 3. Feeding amount of GTS-S

[0102] That is, the maximum feeding amount: 250 tons (coal) × 0.5 wt% = 1.25 tons / hour

[0103] That is, the minimum feeding amount: 130 tons (coal) × 0.1 wt% = 0.13 tons / hour

[0104] Therefore, in one embodiment of the present invention as described above, as the feeding amount of GTS-S, it can be mixed and fed into the coal transferred to the boiler of the thermal power plant in the range of 0.13 tons to 1.25 tons per hour.

[0105] Therefore, by using the automatic feeding system for the catalyst for solid pretreatment desulfurization of the present invention, after automatically and quantitatively feeding the catalyst for solid pretreatment desulfurization (GTS-S) into the coal supply of the thermal power plant as a pretreatment, it can be adsorbed onto the ash generated in the combustion particles during the combustion process of the combustible (coal) to activate its porosity, and efficiently adsorb and remove the sulfur oxides (SOx) present in the ash, thereby achieving the excellent effect of reducing the emission of sulfur oxides before the generation of the exhaust gas.

[0106] That is, the existing flue gas desulfurization method belongs to the method of removing the sulfur oxides (SOx) contained in the generated exhaust gas only after burning the combustible, and has the problems of requiring more desulfurization equipment for performing the process, manpower for operating the desulfurization equipment, and higher costs. However, by using the automatic feeding system for the catalyst for solid pretreatment desulfurization according to the present invention, the catalyst for solid pretreatment desulfurization (GTS-S) is premixed with the combustible before the combustion of the combustible and then burned together, so that the desulfurization catalyst can adsorb and remove the sulfur oxides generated during the combustion of the combustible during the combustion process, and finally an excellent desulfurization effect of reducing the emission of sulfur oxides in the exhaust gas can be achieved.

[0107] While the coal supply is moving on the conveyor, the solid pretreatment desulfurization catalyst is automatically added and mixed in a certain proportion above the conveyor in a manner linked to the weight of the coal supply. Therefore, compared with the existing liquid desulfurization catalyst, it is simpler and easier to add. Moreover, the solid pretreatment desulfurization catalyst (GTS-S) used in the present invention does not have the problem of flowing after being added to the coal supply, which is a problem of the existing liquid desulfurization catalyst. Therefore, the effect of being easily applicable to various combustion facilities can be achieved.

[0108] In addition, the automatic start-up system according to the present invention does not need to separately construct a desulfurization treatment facility for treating the exhaust gas generated after the combustion of coal in a thermal power plant. Instead, by mixing the combustion product with a solid pre-treatment desulfurization catalyst before combustion and then burning it, the economic effect of quickly reducing sulfur oxides at an economical and low cost can be achieved.

[0109] In addition, the combustibles that can be applied to the solid pretreatment desulfurization catalyst according to the present invention can widely include combustibles such as coal, oil, waste and biogas that can release a large amount of heat through combustion, but in one embodiment of the present invention, it is preferably easily applicable to coal.

[0110] In addition, after the solid pretreatment desulfurization catalyst as described above is mixed into the combustible in a certain proportion before combustion and then burned together with the combustible, an excellent desulfurization effect can be maintained by adjusting the mixing amount of the solid pretreatment desulfurization catalyst according to the content of C, H, N and S contained in the combustible.

[0111] It should be noted that the present invention is not limited to the one embodiment described in the above content. Even if the detailed composition or quantity and configuration structure of the device are changed, the same effect can be achieved. Therefore, a person with general knowledge of the technical field to which the present invention belongs can perform the addition, deletion and deformation of various structures within the scope of the technical idea of ​​the present invention.

[0112] Industry availability

[0113] The invention can be widely applied to an automatic input system of a solid pretreatment desulfurization catalyst.

Claims

1. An automatic feeding system for a catalyst for solid pretreatment desulfurization, comprising: A main silo, formed with a plurality of lower discharge ports, receiving the supply of the catalyst for solid pretreatment desulfurization from the open upper feeding port; A plurality of metering silos, located below the main silo, receiving the supply of coal from each of the discharge ports at the lower end of the main silo, and in a state of being respectively disposed above the coal feeding conveyor of a thermal power plant, causing the catalyst for solid pretreatment desulfurization to fall onto the upper part of the coal transported by the coal feeding conveyor, so as to feed the catalyst for solid pretreatment desulfurization into the transported coal; and A sensing control unit, sensing the input amount of the coal transported by the coal feeding conveyor, and controlling the opening and closing of the discharge ports of the metering silos respectively in a manner linked to the sensed input amount of the coal, so as to control the catalyst for solid pretreatment desulfurization to fall and be fed in a certain proportion in direct proportion to the coal input amount.

2. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, On one side of the main silo, there is also included: A vertical transfer assembly for vertically transferring the catalyst for solid pretreatment desulfurization from the ground to the upper feeding port of the main silo.

3. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 2, The vertical transfer assembly is a bucket elevator or a hoist.

4. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, At least one position between the discharge port of the main silo and the input port of the metering silo or between the discharge port of the metering silo and the coal supply conveyor further includes: A horizontal transfer assembly for horizontally transferring the catalyst for solid pretreatment desulfurization.

5. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 4, The horizontal transfer assembly is a screw feeder or a belt conveyor.

6. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, On the outer surface adjacent to the discharge port of the main silo, there is also included: At least one vibrator, applying vibration to prevent the stagnation of the catalyst for solid pretreatment desulfurization discharged through the discharge port of the main silo.

7. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, At the discharge outlet of the main silo or metering silo, there is also included: A rotary valve for controlling the discharge of the catalyst for solid pretreatment desulfurization.

8. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, The sensing control unit includes: A load cell, equipped at the lower end of the coal feeding conveyor, measuring the instantaneous weight of the coal feeding; And A motion detector, equipped above the coal feeding conveyor, measuring the transfer speed of the transported coal feeding.

9. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, The metering silo feeds the catalyst for solid pretreatment desulfurization into the coal feeding at a ratio of 0.1 to 0.5 wt% compared to the weight of the coal feeding transported on the coal feeding conveyor per hour.

10. The automatic feeding system for a catalyst for solid pretreatment desulfurization according to claim 1, The manufacture of the catalyst for solid pretreatment desulfurization includes: (a) A step of manufacturing a liquid pretreatment desulfurization catalyst; Step of crushing a carrier having a porous structure with pores into a certain size; Step of immersing the carrier crushed into a certain size in step (b) into the liquid pretreatment desulfurization catalyst produced in step (a) and impregnating for 10 to 60 minutes; and, Step of drying the carrier at a temperature of 100 °C or higher for a certain period of time after putting the carrier into a dryer in a state where the liquid pretreatment desulfurization catalyst has penetrated into the pores of the carrier through the impregnation in step (c).

11. The automatic feeding system for the solid pretreatment desulfurization catalyst according to claim 10, After the step (d), further comprising: Step of pulverizing the carrier dried in a state where the liquid pretreatment desulfurization catalyst has penetrated into the pores of the carrier by crushing.

12. The automatic feeding system for the solid pretreatment desulfurization catalyst according to claim 11, After the step (e), further comprising: Step of using the solid component manufactured into powder through step (e) as the solid pretreatment desulfurization catalyst, or putting the solid component into an extruder to manufacture pellets, or putting the solid component into a tablet press to manufacture tablets.

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