Patent Application
20170044014
Field
The present disclosure relates to high temperature dry desulfurization system and method using multi regeneration reactor.
Description of the Related Art
High temperature dry desulfurization technology is technology removing sulfur ingredients such as H2S, COS in fuel gas generated from coal gasification or synthetic gas in high temperature with a dry state. The high temperature dry desulfurization technology has an advantage of having no waste water treatment in an environmental aspect compared to low temperature wet desulfurization technology using absorbent of amine type which is widely used in general chemical plant, sulfur ingredient may be removed in high temperatures of 400-600° C., cooling of the synthetic gas may not needed compared to the wet desulfurization technology operated low temperature (below 100° C.), reducing sensible heat, thereby increasing power generation efficiency.
In particular, in the case of Integrated Gasification Combined Cycle (IGCC), sulfur ingredients included fuel gas must be reduced less than dozens of ppmv in order to prevent corrosion of a gas turbine, and in the case of Integrated Gasification Fuel Cell (IGFC) must be reduced to ppbv level in order to prevent poisoning of catalyst and degradation of electrode.
The high temperature dry desulfurization technology is technology which selectively absorbs H2S and COS and removes when high temperature and high pressure fuel gas (or synthetic gas) contacts with desulfurizing agent in a solid state. Composition of synthetic gas emitted by coal gasification may be changed according to type of the coal gasification and composition of coal; however, representatively, composition of synthetic gas emitted by coal gasifier of Shell is 65% of CO, 1.5% of CO2, 29.5% of H2, 4% of N2 and also includes H2S and COS.
As illustrated in
Representatively, in the case that Zinc oxide is used as the desulfurizing agent, within the desulfurization reactor, the sulfur ingredients H2S and COS are absorbed into the desulfurizing agent by reaction such as the following Formula 1 and Formula 2 and are to be emitted H2O or CO2.
H2S+ZnO=ZnS+H2O [Formula 1]
COS+ZnO=ZnS+CO2 [Formula 2]
Further, the desulfurizing agent absorbed the sulfur ingredients and the synthetic gas removed the sulfur ingredients are emitted through outlet 12 of upper portion of desulfurization reactor 10 and flowed into a desulfurization cyclone 20 (S2), and the synthetic gas removed the sulfur ingredients by dividing them into gas and solid in the desulfurization cyclone 20 is emitted through gas outlet 21 of upper portion of the desulfurization cyclone, and desulfurizing agent particles (solid) absorbed the sulfur are emitted through solid outlet 22 of lower portion of the desulfurization cyclone and are introduced in regeneration reactor 30 (S3).
In the regeneration reactor 30, ZnO and SO2 are to be obtained by oxidizing ZnS by injecting oxidizing agent (oxygen or air) to oxidizing agent inlet 32 of lower portion of regeneration reactor as like below Formula 3, and oxidized desulfurizing agent particles recirculate again to the desulfurization reactor by discharging through desulfurizing agent outlet 33.
ZnS+1.5 O2=ZnO+SO2 [Formula 3]
The desulfurizing agent emitted in the regeneration reactor 30, SO2, and other gases are introduced in regeneration cyclone 40 by emitting through regeneration reactor outlet 34 (S4), SO2, and other gases are emitted through gases outlet 41 of upper portion of the regeneration cyclone by dividing air and solid in the regeneration cyclone 40, and the desulfurizing agent recirculates by emitting through solid outlet 42 of lower portion of the regeneration cyclone 40 and is flowed into recirculation inlet 35 of the regeneration reactor (S5).
In addition, SO2 and other gases emitted in the regeneration reactor 30 and emitted through gas outlet of the regeneration cyclone as illustrated in
SO2+2CO=2CO2+S [Formula 4]
SO2+2H2=2H2O+S [Formula 5]
In the sulfur recovery reactor 50, reductive gas CO, H2, etc., which are needed to direct sulfur recovery reaction may be injected separately; however, CO and H2 included the synthetic gas may be used, therefore, as illustrated in
For this high temperature dry desulfurization technology, because desulfurizing agent having solid particles must continuously circulate between the desulfurization reactor 10 and the regeneration reactor 30, fluidized bed type reactor is generally used, and in the case of the direct sulfur recovery process, fixed bed type reactor charged the catalyst is to be used mostly.
In high temperature dry desulfurization apparatus like
In the case of the air injection, air may must be injected as much amount of oxygen needed to regeneration reaction of desulfurizing agent; however, it may be changed only within scope of change of gas velocity of the regeneration reactor 30 to be operated in fluidized bed state, excess oxygen injection is advantageous in order to complete regeneration of the desulfurizing agent, therefore, in gas emitted in the regeneration reactor 30 and flowed into the direct sulfur recovery process the oxygen is to be included with SO2.
In the case that the oxygen is injected in the direct sulfur recovery process, reductive gas which is to be reduced SO2 to element S is consumed because a combustion reaction of CO and H2 as like following Formula 6 and 7 is to be occurred rather than reaction occurred in aforementioned Formula 4 and 5, therefore, sulfur recovery efficiency may be decreased, and the combustion reaction of CO and H2 is the exothermic reaction, and temperature of catalyst layer is to be increased drastically, therefore, decreased activity by thermal shock and deterioration of catalyst may be occurred.
CO+0.5 O2=CO2 [Formula 6]
H2+0.5 O2=H2O [Formula 7]
Therefore, in the case that the oxygen is flowed into the direct sulfur recovery process, efficiency of a catalyst reaction may be decreased and it may influence stability of process, therefore, it is important that minimizing flowed oxygen concentration. However, in order to increase efficiency of regeneration of high temperature dry desulfurization process regeneration reactor 30, high oxygen concentration is advantageous; therefore, method for increasing efficiency of both processes was required.
Therefore, the present disclosure has been made in an effort to overcome the conventional difficulty, according to an exemplary embodiment of the present disclosure, flowing oxygen into the direct sulfur recovery process may be prevented, smooth regeneration of the desulfurizing agent therefrom in the high temperature dry desulfurization process reactor may possible, and supplying high temperature dry desulfurization having multi regeneration reactor which enables to prevent decrease of sulfur recovery efficiency by oxygen injection to direct sulfur recovery process and decreased activity by the deterioration of catalyst, desulfurization system, and operating method thereof are provided.
Meanwhile, technical objects to be achieved in the present disclosure are not limited to the aforementioned technical objects, and other not-mentioned technical objects will be obviously understood by those skilled in the art from the description below.
The present disclosure provides in a desulfurization system removing sulfur ingredients included synthetic gas generated from gasification of coal in a high temperature dry state, a desulfurization reactor removing sulfur ingredients of the synthetic gas by desulfurizing agent; a desulfurization cyclone discharging by separating synthetic gas removed sulfur ingredients discharged in the desulfurization reactor and desulfurizing agent absorbed sulfur ingredients; at least one of a first regeneration reactor branched in the desulfurization cyclone and regenerates the desulfurizing agent absorbed the sulfur ingredients by flowing the desulfurizing agent absorbed the discharged sulfur ingredients; at least one of a second regeneration reactor branched in the desulfurization cyclone and regenerates the desulfurizing agent absorbed the sulfur ingredients by flowing the desulfurizing agent absorbed discharged sulfur ingredients; a first oxidizing agent supplying means injecting oxidizing agent to a first oxidizing agent inlet of the first regeneration reactor, a second oxidizing agent supplying means injecting oxidizing agent to a second oxidizing agent inlet of the second regeneration reactor; a first inlet valve provided at a side of a first regeneration reactor inlet pipe connecting between the desulfurization cyclone and a first solid inlet of the first regeneration reactor, a first outlet valve provided at a first desulfurization outlet of the first regeneration reactor, a second inlet valve provided at a side of a second regeneration reactor inlet pipe connecting between the desulfurization cyclone and a second solid inlet of the second regeneration reactor, a second outlet valve provided at a second desulfurization agent outlet of the second regeneration reactor; a controller operating one of the first regeneration reactor and the second regeneration reactor in a regeneration mode, controlling the other to operate in a desulfurization mode by circulating desulfurizing agent between the desulfurization reactors, in the case of operating the first regeneration reactor in the regeneration mode, closing the first inlet valve and the first outlet valve, operating the first oxidizing agent supplying means, in the case of operating the second regeneration reactor in a regeneration mode, closing the second inlet valve and the second outlet valve, controlling the second oxidizing agent supplying means to operate; a first regeneration cyclone separating gas and solid discharged through a first recirculation outlet of the first regeneration reactor and recirculating the solid through a first recirculation inlet of the first regeneration reactor when the first regeneration reactor operates in a regeneration mode; a second regeneration cyclone separating gas and solid discharged through a second recirculation outlet of the second regeneration reactor recirculating the solid through a second recirculation inlet of the second regeneration reactor when the second regeneration reactor operates in a regeneration mode; a first measuring sensor measuring whether oxygen is discharged in the first regeneration reactor when the first regeneration reactor operates in a regeneration mode; and in the case that the second regeneration reactor operates in the regeneration mode, includes a second measuring sensor which measures whether oxygen is discharged in the second regeneration reactor, the controller determines whether regeneration mode of the first regeneration reactor ceases based on measurement value of the first measuring sensor, determines whether regeneration mode of the second regeneration reactor ceases based on measurement value of the second measuring sensor, in the case that the first regeneration reactor operates in the regeneration mode, gas including desulfurizing agent discharged in the first regeneration reactor and sulfur is flowed into the first regeneration cyclone, the desulfurization agent discharged in solid outlet of the first regeneration cyclone recirculates to the first regeneration reactor, the gas including sulfur is flowed into sulfur recovery reactor, in the case that the second regeneration reactor operates in the regeneration mode, air including desulfurizing agent discharged in the second regeneration reactor and sulfur is flowed into the second regeneration cyclone, the desulfurization agent discharged in solid outlet of the second regeneration cyclone recirculates to the second regeneration reactor, the gas including sulfur is flowed into the sulfur recovery reactor.
In an operating method of the high temperature dry desulfurization system removing sulfur of synthetic gas generated from the gasification of coal in the high temperature dry state, a first stage putting the desulfurizing agent into the desulfurization reactor by opening the first inlet valve of the first regeneration reactor and the first outlet valve, and opening the second inlet valve of the second regeneration valve and the second outlet valve; a second stage operating the first regeneration reactor in the regeneration mode by putting oxidizing agent into the first regeneration reactor by closing the first inlet valve and the first outlet valve and driving the first oxidizing the first oxidizing agent supplying means and progressing desulfurization reaction by circulating the desulfurizing agent between the second regeneration reactor and the desulfurization reactor; a third stage operating the second regeneration reactor in the regeneration mode by putting oxidizing agent into the second regeneration reactor by closing the second inlet valve and the second outlet valve when the regeneration reaction of the first regeneration reactor is ended, and driving the first oxidizing a second oxidizing agent supplying means and progressing desulfurization reaction by circulating the desulfurizing agent between the first regeneration reactor and the desulfurization reactor; a fourth stage repeating the second stage and the third stage.
Further, the first stage provides controlling the controller to close the first inlet valve, the first outlet valve, the second inlet valve, and the second outlet valve, charging the desulfurizing agent in the first regeneration reactor and in the second regeneration reactor; circulating the desulfurizing agent in the first regeneration reactor between the desulfurization reactor by controlling the controller to open the first inlet valve and the first outlet valve; and circulating the desulfurizing agent in the second regeneration reactor between the desulfurization reactor by controlling the controller to open the second inlet valve and the second outlet valve.
In addition, in the second stage, an operating method of the first regeneration reactor operated in the regeneration mode includes regenerating desulfurizing agent by oxidizing agent injected within the first regeneration reactor operated in the regeneration mode; flowing gas including the desulfurizing agent and sulfur into the first regeneration cyclone through the first recirculation outlet of the first regeneration reactor; regenerating the desulfurizing agent by circulating the first regeneration reactor through the solid outlet of the first regeneration cyclone; and recovering sulfur by flowing the gas including sulfur through the gas outlet of the first regeneration cyclone; the operating method of the second regeneration reactor operated in the desulfurization mode includes controlling the sulfur ingredients of the synthetic gas put the desulfurization reactor by flowing the desulfurizing agent within the second regeneration reactor into the desulfurization reactor, flowing the desulfurizing agent absorbed the sulfur ingredients and the synthetic gas removed the sulfur ingredients into the desulfurization cyclone, emitting the synthetic gas removed the sulfur ingredients to the gas outlet of the desulfurization cyclone and circulating the desulfurizing agent absorbed the sulfur ingredients by flowing into the second regeneration reactor.
Further, measuring whether the first measuring sensor of the first regeneration reactor discharges the oxygen in the first regeneration reactor, determining the controller whether the regeneration reaction of the first regeneration reactor is terminated based on the measurement value of the first measuring sensor.
In addition, in the third stage, an operating method of the second regeneration reactor operated in the regeneration mode includes regenerating desulfurizing agent by oxidizing agent injected within the second regeneration reactor operated in the regeneration mode; flowing gas including the desulfurizing agent and sulfur into the second regeneration cyclone through the second recirculation outlet of the second regeneration reactor; regenerating the desulfurizing agent by circulating the second regeneration reactor through the solid outlet of the second regeneration cyclone; and recovering sulfur by flowing the gas including sulfur through the gas outlet of the second regeneration cyclone; the operating method of the first regeneration reactor operated in the desulfurization mode includes controlling the sulfur ingredients of the synthetic gas put the desulfurization reactor by flowing the desulfurizing agent within the second regeneration reactor into the desulfurization reactor, flowing the desulfurizing agent absorbed the sulfur ingredients and the synthetic gas removed the sulfur ingredients into the desulfurization cyclone, emitting the synthetic gas removed the sulfur ingredients to the gas outlet of the desulfurization cyclone and circulating the desulfurizing agent absorbed the sulfur ingredients by flowing into the first regeneration reactor.
Further, measuring whether the second measuring sensor of the second regeneration reactor discharges the oxygen in the second regeneration reactor, determining the controller whether the regeneration reaction of the second regeneration reactor is terminated based on the measurement value of the second measuring sensor.
In accordance with configuration of process and an operating method according to an exemplary embodiment of the present disclosure, the flowing oxygen into the direct sulfur recovery process may be prevented and the smooth regeneration of desulfurizing agent therefrom in the high temperature dry desulfurization process reactor may possible and decreasing of sulfur recovery efficiency by the oxygen injection to the direct sulfur recovery process and decreased activity by the deterioration of the catalyst may be prevented.
Meanwhile, effects to be achieved in the present disclosure are not limited to the aforementioned effects, and other not-mentioned effects will be obviously understood by those skilled in the art from the description below.
The accompanying drawings in the specification illustrate an exemplary embodiment of the present disclosure. The technical spirit of the present disclosure will be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings. Therefore, the present disclosure will not be interpreted to be limited to the drawings:
The above objects, other objects, features and other advantages of the present disclosure will be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings. However, the present disclosure is not limited to the described embodiments, but may be embodied in different ways. On the contrary, exemplary embodiments introduced herein are provided to make disclosed contents thorough and complete and sufficiently transfer the spirit of the present invention to those skilled in the art.
Hereinafter, a configuration and functions, and an operating method of a high temperature dry desulfurization system having multi regeneration reactor 100 will be described. First,
As illustrated in
As illustrated in
In addition, as illustrated in
Further, each the first regeneration reactor 60 and the second regeneration reactor 80 are configured by connecting with a regeneration cyclone 70 and a regeneration cyclone 90. That is, a first recirculation outlet 80 of upper portion of the first regeneration reactor 60 is connected with the first regeneration cyclone 70, desulfurizing agent particles discharged from solid outlet 72 of the first regeneration cyclone 70 recirculate to the first regeneration reactor 60 through a first recirculation inlet 67. In addition, a second recirculation outlet 88 of upper portion of the second regeneration reactor 80 is connected with the second regeneration cyclone 90, desulfurizing agent particles discharged from solid outlet 92 of the second regeneration cyclone 90 recirculate to the second regeneration reactor 80 through a second recirculation inlet 87.
Further, SO2 and other gases discharged gas outlet 71 of the first regeneration cyclone 70 are flowed into the sulfur recovery reactor 50 and SO2 and other gases discharged gas outlet 91 of the second regeneration cyclone 90 are to be flowed into the sulfur recovery reactor 50 as well.
As described hereinafter, the high temperature dry desulfurization system having multi regeneration reactor 100 according to an exemplary embodiment of the present disclosure the first regeneration reactor 60 and the second regeneration reactor 80 are as to be operated alternatively, one of the two regeneration reactors 60 and 80 is used only in solid recirculation in a continuously injectable state of the desulfurizing agent, the other may be used in regeneration reaction, and, besides, it may be performed regeneration reaction by controlling regeneration reaction time. By the configuration of the process and operating method, flow of the oxygen into the sulfur recovery reactor 50 may be prevented.
As described hereinafter, in order to be operated the first regeneration reactor 60 and the second regeneration reactor 80 alternatively, a controller 130 is to be provided oxidizing agent (oxygen or air) within a specific regeneration reactor progressing regeneration reaction by controlling a first oxidizing agent supplying means 110 and a second oxidizing agent supplying means, one of the first regeneration reactor 60 and the second regeneration reactor 80 is to be operated by a regeneration process and the other is to be a solid recirculation process.
In addition, regeneration reaction time is to be controlled by measuring whether the oxygen is contained in gas discharged in the first regeneration reactor 60 in real time by supplying a first measuring sensor 69 at a first recirculation outlet 68 of the first regeneration reactor 60, and regeneration reaction time is to be controlled by measuring whether the oxygen is contained in gas discharged in the second regeneration reactor 80 in real time by supplying a second measuring sensor 89 at a second recirculation outlet 88 of the second regeneration reactor 80.
Hereinafter, an operating method of the high temperature dry desulfurization system having the multi regeneration reactor 100 will be described. First,
First, initially, in a state all closed the first inlet valve 66 and 82 and the first outlet valve 66 and 68, the desulfurizing agent is to be charged in both the first regeneration reactor 60 and the second regeneration reactor 80. (S1)
Further, by opening the first inlet valve 62 and the first outlet valve 66, the desulfurizing agent is to be occurred continuous desulfurization reaction by circulating between the desulfurization reactor 10 and the first regeneration reactor 60 (S12).
As illustrated in
In this case, because the first oxidizing agent supplying means 110 is not operated, the oxidizing agent (oxygen or air) is not injected through the first oxidizing agent inlet 64 of lower portion of the first regeneration reactor 60 and the desulfurizing agent is to be transferred from the first regeneration reactor 60 to the desulfurization reactor 10 by gravity.
Further, the desulfurizing agent charged in the second regeneration reactor 80 is to be flowed into side of the desulfurization reactor 10 after the desulfurizing agent absorbs sulfur in the desulfurization reactor 10. In this case, because the second oxidizing agent supplying means 120 is not operated, the oxidizing agent (oxygen or air) is not injected through the second oxidizing agent inlet 84 of lower portion of the second regeneration reactor 80 and the desulfurizing agent is to be transferred from the second regeneration reactor 80 to the desulfurization reactor 10 by gravity (S13).
Further, after the desulfurizing agent is transferred from the second regeneration reactor 80 to the desulfurization reactor 10, the first regeneration reactor 60 is to be isolated the first regeneration reactor 60 from continuous solid flow by closing the first inlet valve 62 and the first outlet valve 66 (S14).
Then, the controller 130 is to be progress the regeneration reaction within the first regeneration reactor 60 by injecting the oxidizing agent (oxygen or air) through the first oxidizing agent inlet 64 provided at lower portion of the first regeneration reactor 60 by operating the first oxidizing agent supplying means 110.
As illustrated in
That is, in the first regeneration reactor 60 closed the first inlet valve 62 and the first outlet valve 66, the regeneration reaction of aforementioned Formula 3 is to be progress by supplying the oxidizing agent (oxygen or air) through the first oxidizing inlet 64, the desulfurizing agent, SO2, and other gases are discharged through the first recirculation outlet 68 of the first regeneration reactor 60 and are to be introduced in the first regeneration cyclone 70. Further, in the first regeneration cyclone 70, gas and solid are divided, the SO2 and other gases are discharged through the gas outlet 71 of the first regeneration cyclone 70 and are to be flowed into the sulfur recovery reactor 50. Further, the desulfurizing agent recirculates again through the first recirculation inlet 67 to the first regeneration reactor 60.
In addition, SO2 flowed into the sulfur recovery reactor 50 is to be recovered through the sulfur outlet 52 by the catalyst and reaction of aforementioned Formula 4 and 5. Further, while the regeneration reaction is occurred in the first regeneration reactor 60, the desulfurizing agent is to be progress the desulfurization process by circulating the desulfurization reactor 10 and the second regeneration reactor 80 and absorbing the sulfur ingredients.
The first regeneration reactor 60 is operated by the regeneration process, in the case of the second regeneration reactor 80, an operated time for desulfurization reaction may be calculated based on an amount of the sulfur ingredients absorbed in the desulfurization reactor 10 and a solid charging amount of the regeneration reactor, and is to be progress until not emitting oxygen condition (S15). That is, the first measuring sensor 69 is to be measured this condition in real time, in the case that corresponding to condition to be emitted the oxygen, the controller 130 switches its mode.
That is, if the mode is switched, on the contrary to
In other words, when the regeneration reaction time in the first regeneration reactor 60 is ended, after blocking oxidizing agent injection through the first oxidizing agent inlet 64 by stopping operation of the first oxidizing agent supplying means 110, regenerated desulfurizing agent by opening the first inlet valve 62 and the first outlet valve 66 is to be provided to the desulfurization reactor 10 through the first desulfurizing agent outlet 65, and the second reaction reactor 80 is to be isolated from continuous solid flow by closing the second inlet valve 82 and the second outlet valve 86 simultaneously (S16).
That is, the desulfurizing agent is to be regenerated by a reaction as like Formula 3 within the second regeneration reactor 80 by injecting the oxidizing agent (oxygen or air) to the second oxidizing agent inlet 84 of the second regeneration reactor 80 by operating the second oxidizing agent supplying means 120, the desulfurizing agent, SO2, and other gases are discharged through the second recirculation outlet 68 of the second regeneration reactor 80 and are to be introduced in the second regeneration cyclone 90. Further, the air and the solid are divided in the second regeneration cyclone 90, the SO2, and other gases are discharged to the gas outlet 91 and to be flowed into the sulfur recovery reactor 50. Further, the desulfurizing agent recirculates to the second regeneration reactor 80 through the second recirculation inlet 87.
Also, SO2 flowed into the sulfur recovery reactor 50 and sulfur is to be recovered through the sulfur outlet 52 by the catalyst and the reaction of aforementioned Formula 4 and 5. Further, while the regeneration reaction is occurred in the second regeneration reactor 80, the desulfurizing agent is to be progress the desulfurization process by circulating the desulfurization reactor 10 and the first regeneration reactor 60 and absorbing the sulfur ingredients (S17).
The second regeneration reactor 80 is operated by the regeneration process, in the case of the first regeneration reactor 60, an operated time for desulfurization reaction may be calculated based on an amount of the sulfur ingredients absorbed in the desulfurization reactor 10 and a solid charging amount of the regeneration reactor, and is to be progress until not emitting oxygen condition.
As
In other words, the first measuring sensor 69 is to be measured the amount of the sulfur ingredients absorbed in the desulfurization reactor 10 and the solid charging amount of the first regeneration reactor 60, whether to emitting oxygen in the first regeneration reactor 60, and the controller 130 is to be determined whether the regeneration mode of the first regeneration reactor 60 continues based on the measurement value thereof.
The second measuring sensor 89 also measures value required to end of regeneration reaction time in the case that the second regeneration reactor 80 progresses the regeneration reaction. In other words, the second measuring sensor 89 is to be measured the amount of the sulfur ingredients absorbed in the desulfurization reactor 10 and the solid charging amount of the second regeneration reactor 80, whether to emitting oxygen in the second regeneration reactor 80, and the controller 130 is to be determined whether the regeneration mode of the second regeneration reactor 80 continues based on the measurement value thereof.
Further, the controller 130 is to be operated by switching the system 100 to mode by controlling operation of the first oxidizing agent supplying means 110, the second oxidizing agent supplying means 120, the first inlet valve 62, the first outlet valve 66, the second inlet valve 82, and the second outlet valve 86. In other words, the desulfurization reaction is progressed by circulating the solid between the first regeneration reactor 60 and the desulfurization reactor 10, the second regeneration reactor 80 operates in order that the regeneration reaction is to be operated, the controller 130 opens the first inlet valve 62 and the first outlet valve 66, closes the second inlet valve 82 and the second outlet valve 86, and controls to be operated the second oxidizing agent supplying means 120. In addition, desulfurization reaction is progressed by circulating the solid between the second regeneration reactor 80 and the desulfurization reactor 10, the first regeneration reactor 60 operates in order that the regeneration reaction is to be operated, the controller 130 opens the second inlet valve 82 and the second outlet valve 86, closes the first inlet valve 62 and the first outlet valve 66, and controls to be operated the first oxidizing agent supplying means 110.
Further, in the apparatus and the method thereof described above, the configuration and method of embodiments as described above may not be applied with limitation, but the embodiments may be configured by selectively combining all or a part of each embodiment such that various modifications may be made.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10-2015-0113195 | Aug 2015 | KR | national |
